Fixed bed hydroprocessing methods and systems and methods for upgrading an existing fixed bed system

ABSTRACT

A fixed bed hydroprocessing system, and also a method for upgrading a pre-existing fixed bed hydroprocessing system, involves preliminarily upgrading a heavy oil feedstock in one or more slurry phase reactors using a colloidal or molecular catalyst and then further hydroprocessing the upgraded feedstock within one or more fixed bed reactors using a porous supported catalyst. The colloidal or molecular catalyst is formed by intimately mixing a catalyst precursor composition into a heavy oil feedstock and raising the temperature of the feedstock to above the decomposition temperature of the precursor composition to form the colloidal or molecular catalyst in situ. Asphaltene or other hydrocarbon molecules otherwise too large to diffuse into the pores of the fixed bed catalyst can be upgraded by the colloidal or molecular catalyst. One or more slurry phase reactors may be built and positioned upstream from one or more fixed bed reactors of a pre-existing fixed bed system and/or converted from one or more pre-existing fixed bed reactors.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit under 35 U.S.C. § 119 of U.S. provisional application Ser. No. 60/566,269, filed Apr. 28, 2004, and also U.S. provisional application Ser. No. 60/566,254, filed Apr. 28, 2004, the disclosures of which are incorporated herein in their entirety.

BACKGROUND OF THE INVENTION

1. The Field of the Invention

The invention involves methods and systems for hydroprocessing heavy oil feedstocks that include a significant quantity of asphaltenes and fractions boiling above 524° C. (975° F.) to yield lower boiling, higher quality materials. The invention specifically relates to fixed bed hydroprocessing methods and systems that employ a colloidal or molecular catalyst and a porous supported catalyst, and methods for upgrading an existing fixed bed system, to better handle lower quality feedstocks and inhibit formation of coke precursors and sediment and/or extend the life of the supported catalyst.

2. The Relevant Technology

World demand for refined fossil fuels is ever-increasing and will inevitably outstrip the supply of high quality crude oil, whether as a result of actual shortages or due to the actions of oil cartels. In either case, as the price or shortage of crude oil increases there will be an every-increasing demand to find ways to better exploit lower quality feedstocks and extract fuel values therefrom. As more economical ways to process lower quality feedstocks become available, such feedstocks may possibly catch, or even surpass, higher quality crude oils, in the not-too-distant future, as the primary source of refined fossil fuels used to operate automobiles, trucks, farm equipment, aircraft, and other vehicles that rely on internal combustion.

Lower quality feedstocks are characterized as including relatively high quantities of hydrocarbons that have a boiling point of 524° C. (975° F.) or higher. They also contain relatively high concentrations of sulfur, nitrogen and metals. High boiling fractions typically have a high molecular weight and/or low hydrogen/carbon ratio, an example of which is a class of complex compounds collectively referred to as “asphaltenes”. Asphaltenes are difficult to process and commonly cause fouling of conventional catalysts and hydroprocessing equipment.

Examples of lower quality feedstocks that contain relatively high concentrations of asphaltenes, sulfur, nitrogen and metals include heavy crude and oil sands bitumen, as well as bottom of the barrel and residuum left over from conventional refinery process (collectively “heavy oil”). The terms “bottom of the barrel” and “residuum” (or “resid”) typically refer to atmospheric tower bottoms, which have a boiling point of at least 343° C. (650° F.), or vacuum tower bottoms, which have a boiling point of at least 524° C. (975° F.). The terms “resid pitch” and “vacuum residue” are commonly used to refer to fractions that have a boiling point of 524° C. (975° F.) or greater.

By way of comparison, Alberta light crude contains about 9% by volume vacuum residue, while Lloydminster heavy oil contains about 41% by volume vacuum residue, Cold Lake bitumen contains about 50% by volume vacuum residue, and Athabasca bitumen contains about 51% by volume vacuum residue. Resid contains even higher concentrations of fractions that boil at or above about 343° C. (650° F.), with vacuum tower bottoms almost exclusively comprising fractions that boil at or above about 524° C. (975° F.).

Converting heavy oil into useful end products requires extensive processing, including reducing the boiling point of the heavy oil, increasing the hydrogen-to-carbon ratio, and removing impurities such as metals, sulfur, nitrogen and high carbon forming compounds. Examples of catalytic hydrocracking processes using conventional supported catalysts to upgrade atmospheric tower bottoms include fixed-bed hydroprocessing, ebullated- or expanded-bed hydroprocessing, and moving-bed hydroprocessing. Noncatalytic processes used to upgrade vacuum tower bottoms include thermal cracking, such as delayed coking and Flexicoking, and solvent extraction. Solvent extraction is quite expensive and incapable of reducing the boiling point of the heavy oil. Existing commercial catalytic hydrocracking processes involve rapid catalyst deactivation and high catalyst cost, making them currently unsuitable for hydroprocessing vacuum tower bottoms unless substantially diluted with lower boiling fractions, such as atmospheric tower bottoms. Most existing ebullated bed processes operate at less than 65 wt % conversion, while most fixed bed processes have less than about 25 wt % conversion.

A major cause of catalyst and equipment fouling is the undesired formation of coke and sediment, which often results when asphaltenes are heated to the high temperatures required to effect catalytic and thermal cracking. Supported catalysts used in commercial hydrocracking processes such as fixed-bed and ebullated-bed processes utilize solid supported catalysts that include clusters of catalytic sites located within pores or channels in the support material. Most heavy oil feedstocks contain a significant portion of asphaltene molecules, which are either too large to enter the pores of the catalyst support or else become trapped within the pores. Asphaltene molecules that become trapped in the pores deactivate the catalyst sites in the blocked pores. In this way, smaller asphaltene molecules can progressively block all catalyst sites, entirely deactivating the catalyst.

Moreover, larger asphaltene molecules form free radicals, just like other hydrocarbon molecules in the feedstock, but, unlike smaller molecules in the feedstock, are too large to enter the catalyst pores. Because of this, they are generally unable to react with hydrogen radicals located at the catalyst sites. As a result, the larger asphaltene free radicals are free to react with asphaltene and other free radicals in the feedstock, thereby forming larger molecules which continue increasing in size that can foul both the catalyst and the hydroprocessing equipment through the formation of coke precursors and sediment. The tendency of asphaltenes to form coke and sediment increases as the conversion level of the residuum increases due to the more strenuous conditions required to increase conversion. The undesirable reactions and fouling involving asphaltene greatly increase the catalyst and maintenance costs of ebullated-bed and fixed-bed hydrocracking processes. They also render existing commercial processes unsuitable for hydroprocessing vacuum tower bottoms and other very low quality feedstocks rich in asphaltenes.

Exacerbating the relatively low conversion levels using fixed bed hydroprocessing systems is the inability to proportionally convert the asphaltene fraction at the same conversion level as the heavy oil as a whole. Even though ebullated bed hydroprocessing systems are able to operate at substantially higher conversion levels than fixed bed systems, disproportional conversion of asphaltenes relative to the heavy oil as a whole is also problem with ebullated systems. The result of disproportional conversion is a progressive buildup of asphaltenes in the processed feedstock, with an attendant increase in the likelihood that coke and sediment will form in the reactor and other processing equipment.

Another problem involves the formation and continued reaction of free radicals outside the porous supported catalyst within a fixed bed reactor. In general, the beneficial upgrading reactions occur within the pores of the supported catalyst where the active metal catalyst particles are located. Asphaltenes and other larger molecules contained within heavy oil that are too larger to enter the pores of the solid catalyst may form free radicals that are unable to be capped with hydrogen and which can therefore react with other free radicals to yield even larger molecules. They can also form coke and sediment within the reactor, which can plug up or otherwise foul the reactor and/or porous supported catalyst, leading to a pressure drop within the fixed bed reactor.

Another issue unique to fixed bed hydroprocessing systems is the need to remove heat that is generated as the feedstock travels down through the catalyst bed and undergoes hydroprocessing reactions. Unlike ebullated bed reactors in which there is continuous mixing of the feedstock, catalyst and hydrogen, the static nature of fixed bed reactors leads to localized temperature buildups or overheating that might cause undesirable reactions (e.g., equipment and/or catalyst fouling). Cool hydrogen is typically injected into reactor between the layers of catalyst in order to cool the feedstock to prevent overheating and undesirable reactions this might cause.

Another problem associated with conventional fixed bed hydrocracking processes are generally low conversion levels, which are due in part to the tendency of the catalytic activity of the supported catalyst to diminish over time. Moreover, the tendency of asphaltenes or other large molecules within a heavy oil feedstock to foul the fixed bed reactor and/or the need to control the temperature within the fixed bed reactor as discussed above require operating the reactor at relatively low conversion levels (e.g., typically below about 25%) to prevent fouling of the equipment and/or porous supported catalyst. Once the catalytic activity of the catalyst is diminished, the only way to increase catalytic activity is to replenish the old catalyst with new catalyst, which generally requires the complete shut down of the fixed bed reactor at considerable cost. Even with newly replenished catalyst, the conversion level of typical fixed bed systems is substantially lower than ebullated bed systems.

In view of the foregoing, there is an ongoing need to provide improved fixed bed hydroprocessing systems and/or improve (i.e., modify) existing fixed bed systems to overcome one or more of the foregoing deficiencies.

SUMMARY OF THE INVENTION

The present invention relates to fixed bed hydroprocessing methods and system for improving the quality of a heavy oil feedstock that employ both a colloidal or molecular catalyst and a porous supported catalyst. The invention also includes methods for upgrading an existing fixed bed hydroprocessing system by augmenting or replacing at least a portion of the porous supported catalyst with a colloidal or molecular catalyst. The colloidal or molecular catalyst overcomes at least some of the problems associated with the use of porous supported catalysts in upgrading heavy oil feedstocks. These include more effective processing of asphaltene molecules, a reduction in the formation of coke precursors and sediment, reduced equipment fouling, increased conversion levels, enabling the hydroprocessing system to process a wider range of lower quality feedstocks, longer operation in between maintenance shut downs, and more efficient use of the supported catalyst if used in combination with the colloidal or molecular catalyst. Reducing the frequency of shutdown and startup of process vessels means less pressure and temperature cycling of process equipment, and it significantly increases the process on-stream time to produce valuable upgraded products.

Conventional fixed bed hydroprocessing systems typically include one or more fixed bed reactors that comprise a reaction chamber, a port at the top of the reaction chamber through which a heavy oil feedstock and pressurized hydrogen gas are introduced, a plurality of vertically stacked and spaced-apart catalyst beds (e.g., 2 or 3), and a port at the bottom of the reaction chamber through which an upgraded feedstock is withdrawn from the reaction chamber. The catalyst beds are packed with a porous supported catalyst. Catalyst free zones not only exist above and below each catalyst bed, but effectively anywhere outside the pores of the supported catalyst. A distributor plate above each catalyst bed helps to more evenly distribute the flow of feedstock downward through the catalyst beds. Auxiliary ports in the center and/or bottom of the fixed bed reactor may be provided through which a cooling oil or hydrogen quench can be introduced before the partially processed feedstock enters the next catalyst bed to cool heat generated by the hydroprocessing reactions, control the reaction rate, and thereby help prevent formation of coke precursors and sediment and/or excessive gas.

All or substantially all of the beneficial upgrading reactions occur within the catalyst beds since they are the only places within the fixed bed reactor where the heavy oil feedstock, hydrogen and porous supported catalyst exist together. Even within the catalyst beds, the beneficial upgrading reactions occur primarily or exclusively within the pores of the supported catalyst. The heavy oil molecules within the feedstock undergo thermal cracking and hydrotreating reactions within the fixed bed reactor. The hydrocracked molecules diffuse into the pores of the porous supported catalyst where the free radical ends are catalytically reacted with hydrogen, thereby forming stable hydrocarbons of reduced molecular weight and boiling point. Unfortunately, larger molecules that cannot diffuse into the pores of the fixed bed catalyst continue undergoing thermal cracking reactions outside the catalyst so as to form free radicals that have the potential of reacting with other free radicals to produce coke precursors and sediment within the fixed bed reactor and/or within downstream processing equipment.

Moreover, asphaltenes and/or other heavy oil molecules that are too large to enter the pores of the supported catalyst can form coke precursors and sediment within the catalyst beds, potentially fouling and/or prematurely deactivating the catalyst (e.g., by plugging the pores of the catalyst and/or agglomerating porous supported catalyst particles together to form catalyst balls), plugging the interstices between catalyst pellets, causing severe pressure drop and feed throughput in the reactor. Asphaltene free radicals often also leave behind trace metals such as vanadium and nickel in the catalyst pores, gradually reducing the pore diameter and preventing further access by other hydrocarbon molecules or radicals. For the foregoing reasons, it is very difficult to upgrade heavy oil feedstocks rich in asphaltenes (e.g., vacuum tower bottoms) using conventional fixed bed hydroprocessing systems because they tend to quickly foul and/or deactivate such systems.

The present invention provides improved fixed bed hydroprocessing methods and systems that more effectively process lower quality heavy oil feedstocks. The fixed bed hydroprocessing methods and systems of the invention employ a dual hydroprocessing catalyst system comprising a colloidal or molecular catalyst and a porous supported catalyst, typically within separate reactors but also possibly within the same reactor so long as the supported catalyst is designed so as to not remove the colloidal molecular catalyst from the feedstock being processed.

According to a typical embodiment, one or more slurry phase reactors a containing the colloidal or molecular catalyst are used to preliminarily hydroprocess the heavy oil feedstock, including a substantial portion of asphaltenes or other molecules that may be too large to enter the pores of the porous supported catalyst, prior to introducing the preliminarily upgraded feedstock into one or more fixed bed reactors. In one embodiment, the first fixed bed reactor will be a guard bed that acts to remove the colloidal or molecular metal sulfide catalyst and metal impurities native to the heavy oil feedstock in order to prevent or inhibit plugging and/or deactivation of the porous supported catalyst within one or more downstream fixed bed reactors. It is also within the scope of the invention to utilize the colloidal or molecular catalyst in combination with a porous supported catalyst within a fixed bed reactor, though this may require modifying typical fixed bed catalysts in order to not remove, and therefore become plugged up with, the colloidal or molecular catalyst.

One or more hot separators may be positioned at various points within the system in order to remove gases and volatile liquids from the non-volatile liquid fraction, which is then processed in one or more downstream hydroprocessing reactors. A guard bed may be used to remove metals and other impurities and/or the colloidal or molecular catalyst prior to further processing of the feedstock into final usable products. Where it is desired to recycled a heavy resid fraction back through the hydroprocessing system, it may be advantageous to leave the colloidal or molecular catalyst within the resid fraction. The colloidal or molecular catalyst generally does not become deactivated and can be used to catalyze beneficial upgrading reactions within the recycled resid fraction without having to add completely new catalyst.

According to one embodiment, a colloidal or molecular catalyst is formed and/or a well-dispersed catalyst precursor composition is incorporated within a heavy oil feedstock prior to introducing the feedstock into at least at least one of a slurry phase or fixed bed reactor. The well-dispersed catalyst precursor composition is able to form the colloidal or molecular catalyst in situ in the feed heaters and/or within the fixed bed or slurry phase reactor. One benefit of the colloidal or molecular catalyst is that it provides catalytic activity in addition to the porous supported catalyst.

In the case of heavy oil feedstocks that include asphaltenes, a significant portion of the colloidal-sized particles or molecules of the polar hydroprocessing catalyst become associated with the more hydrophilic asphaltene molecules. As the asphaltene molecules form free radicals during thermal cracking, the closely associated colloidal catalyst particles or molecules catalyze a reaction between the asphaltene radicals and hydrogen, thereby preferentially promoting beneficial upgrading reactions to form smaller hydrocarbon molecules that contain less sulfur instead of forming coke precursors and sediment. As a result, the asphaltene fraction found in heavy oil feedstocks can be upgraded into more usable materials along with other hydrocarbons in the feedstock rather than simply being a coke and sediment precursor that is, at best, a waste product that must be disposed of and, at worst, a nemesis that can quickly deactivate the porous supported catalyst and/or foul the fixed bed hydroprocessing system, requiring substantially greater quantities of catalyst and/or costly shut downs and clean-up operations. Repeatedly shutting down pressurized vessels involving high temperature and high pressure cyclings can greatly reduce the on-stream availability of the processing equipment.

When the colloidal or molecular catalyst is used in one or more slurry phase reactors upstream from one or more fixed bed reactors, upgrading reactions within the slurry phase reactor convert the asphaltenes or other larger hydrocarbon molecules into smaller molecules able to enter the pores of the supported catalyst within the fixed bed reactor. In this way, the colloidal or molecular catalyst can be employed to preliminarily upgrade a lower quality heavy oil feedstock into a higher quality feedstock comprising smaller hydrocarbon molecules of lower molecular weight that can be more effectively hydroprocessed by the porous supported catalyst of the fixed bed reactor. This reduces fouling of the fixed bed reactor and downstream equipment and increases the lifespan of the porous supported catalyst. In the case where all or substantially all of the asphaltenes and/or other large molecules within the heavy oil feedstock are preliminarily converted in one or more slurry phase reactors containing the colloidal or molecular catalyst, the fixed bed reactors may be used primarily or solely to perform relatively mild or less severe hydrotreating reactions.

If used in combination with a porous supported catalyst in a fixed bed reactor, the colloidal or molecular catalyst helps promote catalytic upgrading reactions in place of detrimental reactions between hydrocarbon free radicals that might otherwise occur outside of the catalyst beds and/or porous supported catalyst of the fixed bed reactor. The colloidal or molecular catalyst is able to promote beneficial upgrading reactions involving asphaltenes or other hydrocarbon molecules that are too large to diffilse into the pores of the porous supported catalyst. This reduces or eliminates the incidence of catalyst fouling, such as plugging the catalyst pores and/or catalyst balling, and/or formation of coke precursors and sediment that might otherwise foul the fixed bed reactor and downstream equipment.

The methods and systems according to the invention may employ other processing equipment as desired upstream and/or downstream from one or more fixed bed reactors. Examples of other processing equipment that may be incorporated within the fixed bed hydroprocessing systems of the invention include one or more of a preheating chamber, such as for causing the well dispersed catalyst precursor composition to decompose and/or for causing the heavy oil feedstock to liberate sulfur that can combine with the metal liberated from the catalyst precursor composition, a slurry phase reactor, an ebullated bed reactor, an atmospheric distillation tower, a vacuum distillation tower, a scrubber, an aqueous washing system, and conduits and channels for transporting the feedstock from one location in the system to another.

The colloidal or molecular catalyst within the heavy oil feedstock is typically formed in situ within the heavy oil feedstock prior to, or upon introducing the feedstock into a slurry phase and/or fixed bed reactor. According to one embodiment, an oil soluble catalyst precursor composition comprising an organo-metallic compound or complex is blended with the heavy oil feedstock containing sulfur bearing molecules and thoroughly mixed in order to achieve a very high dispersion of the precursor composition within the feedstock prior to formation of the catalyst. An exemplary catalyst precursor composition is a molybdenum 2-ethylhexanoate complex containing approximately 15% by weight molybdenum.

In order to ensure thorough mixing of the precursor composition within the feedstock, the catalyst precursor composition is preferably preblended with a hydrocarbon oil diluent (e.g., vacuum gas oil, decant oil, cycled oil, or light gas oil) to create a diluted precursor mixture, which is thereafter blended with the heavy oil feedstock. The decomposition temperature of the catalyst precursor composition is selected so as to be sufficiently high so that the catalyst precursor composition resists substantial premature decomposition before intimate mixing of the catalyst precursor composition within the feedstock has been achieved. Subsequent heating of the feedstock to a temperature sufficient to cause the release of hydrogen sulfide from sulfur-bearing hydrocarbon molecules, either before or upon commencing hydroprocessing, causes the catalyst precursor composition that has been intimately mixed with the feedstock to yield individual metal sulfide catalyst molecules and/or extremely small particles that are colloidal in size (i.e., less than 100 nm, preferably less than about 10 nin, more preferably less than about 5 nm, and most preferably less than about 1 nm).

Once formed, the metal sulfide catalyst compound, being dissociated from the oil soluble portion of the catalyst precursor, is highly polar. On the other hand, oil feedstocks are very hydrophobic, making it impossible to disperse larger hydrophilic metal sulfide catalyst particles into smaller-sized particles within the feedstock, let alone so as to yield a colloidal or molecular dispersion of catalyst. This is true whether the metal catalyst compound is added directly to the oil feedstock as a solid powder or as part of an aqueous solution instead of using an oil soluble catalyst precursor composition as in the present invention to form the catalyst compound in situ within the feedstock. It is for this reason that the oil soluble precursor composition is intimately mixed with the feedstock before decomposition of the catalyst precursor composition and formation of the catalyst compound.

If the oil soluble catalyst precursor composition is well mixed throughout the heavy oil feedstock before decomposition, the metal catalyst atoms and/or metal catalyst compounds will be physically separated from each other and surrounded by the heavy oil feedstock molecules, which is believed to prevent or inhibit substantial agglomeration. It has been found that preblending the catalyst precursor composition with a hydrocarbon diluent prior to blending the resulting diluted precursor mixture within the feedstock greatly aids in ensuring that thorough blending of the precursor composition within the feedstock occurs before decomposition of the precursor composition to yield the catalyst, particularly in the case of large-scale industrial applications. The result of thorough mixing is that all, or a substantial portion, of the catalyst precursor composition is converted into individual metal sulfide molecules, or particles colloidal in size, instead of larger metal sulfide particles comprising a large number of metal sulfide compounds joined together. On the other hand, failure to intimately blend the oil soluble precursor composition into the feedstock before decomposition of the precursor results in the formation of larger catalyst particles (i.e., micron-sized or greater) comprising a relatively large number of metal sulfide molecules joined together rather than a molecular or colloidal dispersion of the metal sulfide catalyst.

Notwithstanding the generally hydrophobic nature of heavy oil feedstocks, because asphaltene molecules generally have a large number of oxygen, sulfur and nitrogen functional groups, as well as associated metal constituents such as nickel and vanadium, the asphaltene fraction is significantly less hydrophobic and more hydrophilic than other hydrocarbons within the feedstock. Asphaltene molecules therefore generally have a greater affinity for the polar metal sulfide catalyst, particularly when in a colloidal or molecular state, compared to more hydrophobic hydrocarbons in a heavy oil feedstock. As a result, a significant portion of the polar metal sulfide molecules or colloidal particles tend to become associated with the more hydrophilic and less hydrophobic asphaltene molecules compared to the more hydrophobic hydrocarbons in the feedstock. The close proximity of the catalyst particles or molecules to the asphaltene molecules helps promote beneficial upgrading reactions involving free radicals formed through thermal cracking of the asphaltene fraction. This phenomenon is particularly beneficial in the case of heavy oils that have a relatively high asphaltene content, which are otherwise difficult, if not impossible, to upgrade using conventional hydroprocessing techniques due to the tendency of asphaltenes to deactivate porous supported catalysts and deposit coke and sediments on or within the processing equipment. In the case of conventional fixed bed hydroprocessing systems, the asphaltene content may generally not exceed 10% by volume of the feedstock.

According to one embodiment, metal-catalyst atoms liberated from the organo-metallic precursor compound or complex react with sulfur liberated from the heavy oil feedstock during heating to yield metal catalyst compounds that comprise one or more types of metal sulfides. A non-limiting example of a useful metal sulfide catalyst that may be employed in the methods and systems according to the invention is molybdenum disulfide. A non-limiting example of a catalyst precursor composition used to form molybdenum disulfide is molybdenum 2-ethyl hexanoate.

The molecular or colloidal catalyst generally never becomes deactivated because it is not contained within the pores of a support material. Moreover, because of intimate contact with the heavy oil molecules, the molecular or colloidal catalyst particles can rapidly catalyze a hydrogenation reaction between hydrogen atoms and free radicals formed from the heavy oil molecules. Although the molecular or colloidal catalyst leaves the reactor with the upgraded product, it is constantly being replaced with fresh catalyst contained in the incoming feedstock. As a result, process conditions, throughput and conversion levels remain significantly more constant over time compared to fixed bed processes that utilize a porous supported catalyst as the sole hydroprocessing catalyst. Moreover, because the molecular or colloidal catalyst is more freely dispersed throughout the feedstock, including being intimately associated with asphaltenes, conversion levels and throughput are significantly or substantially increased compared to conventional fixed bed hydroprocessing systems.

The more uniformly dispersed molecular or colloidal catalyst is also able to more evenly distribute the catalytic reaction sites throughout the reaction chamber and feedstock. This reduces the tendency for free radicals to react with one another to form coke precursor molecules and sediment compared to conventional fixed bed reactors that only use a relatively large (e.g., ¼″×⅛″ or ¼″× 1/16″) (6.35 mm×3.175 mm or 6.35 mm×1.5875 mm) supported catalyst, wherein the heavy oil molecules must diffuse into the pores of catalyst support to reach the active catalyst sites.

In another aspect of the invention, an existing fixed bed hydroprocessing system be upgraded by augmenting the supported catalyst with the colloidal or molecular catalyst described herein. Fixed bed hydroprocessing systems typically cost millions of dollars to build. Rather than dismantling such systems, or building entirely new hydroprocessing systems at great cost to accommodate low quality heavy oil feedstocks that are rich in asphaltenes and/or high boiling fractions (e.g., above 975° F.), the present invention provides a method for modifying a pre-existing fixed bed hydroprocessing system so that it can more effectively process lower quality heavy oil feedstocks.

According to one embodiment, a pre-existing fixed bed hydroprocessing system comprising one or more fixed bed reactors can be upgraded by constructing one or more new slurry phase reactors upstream from one or more fixed bed reactors in order to preliminarily upgrade a heavy oil feedstock. The new slurry phase reactor(s) will include a liquid phase comprising a heavy oil feedstock and the colloidal or molecular catalyst and a gaseous phase comprising hydrogen gas. The preliminarily upgraded feedstock produced by the one or more slurry phase reactors in the presence of the colloidal or molecular catalyst will contain a substantially reduced quantity of asphaltenes and/or other molecules that would otherwise be large to enter the pores of the porous supported catalyst utilized in a fixed bed reactor. This has the effect of prolonging the life of the downstream fixed bed reactors and/or improving the ability of the upgraded fixed bed hydroprocessing system to treat lower quality heavy oil feedstocks having higher concentrations of asphaltenes or other large molecules that might otherwise foul or plug the fixed bed reactors and/or porous supported catalyst. The number and/or conversion level of the one or more slurry phase reactors can be adjusted depending on the quality of the heavy oil feedstock being hydroprocessed in.

Instead of, or in addition to, constructing one or more new slurry phase reactors upstream from one or more fixed bed reactors as discussed above, one or more fixed bed reactors of a pre-existing fixed bed hydroprocessing system comprising multiple fixed bed reactors can be converted into slurry phase reactors. This is accomplished by removing the porous supported catalyst from a fixed bed reactor and replacing it with the colloidal or molecular catalyst described herein. In one embodiment, the fixed bed reactor can be further modified by incorporating a recycle cup, recycle pump and distributor grid plate, such as may be found in a conventional ebullated bed reactor, in order to improve the distribution of reactants and heat throughout the converted reactor.

In the case where one or more guard beds are positioned upstream from the one or more fixed bed reactors being converted into a slurry phase reactor, the feedstock will typically be re-routed so as to bypass the guard bed(s) before being introduced into the converted reactors. The upgraded material produced by the converted reactors may then be routed to the guard bed(s) in order to remove the colloidal or molecular catalyst and/or metal contaminants within the upgraded material prior to introducing the cleaned material into one or more downstream fixed bed reactors (e.g., for hydrotreating).

In another embodiment, a pre-existing fixed bed hydroprocessing reactor system comprising one or more fixed bed reactors can be upgraded by incorporating a colloidal or molecular catalyst within the heavy oil feedstock and then introducing the feedstock into one or fixed beds, typically upstream from the guard bed(s), which may require re-routing so as to reposition the sequence or order of the various fixed bed reactors. Incorporating the colloidal or molecular catalyst within the heavy oil feedstock as a co-catalyst would be expected to increase the useful lifespan of the porous supported catalyst in the one or more fixed bed reactors, thereby increasing the time before the fixed bed(s) must be shut down in order to replace the spent supported catalyst with fresh catalyst. This has the beneficial effect of reducing down time and the porous supported catalyst requirement. The more evenly distributed catalytic sites also increases the conversion level, while reducing or eliminating the tendency of free radicals to react together to form coke precursors and sediment.

A guard bed may be included downstream from one or more slurry phase reactors and upstream from one or more fixed bed reactors in order to remove metals and other impurities so as to prolong the lifespan of the supported catalyst in the fixed bed reactors. It is also within the scope of the invention to use the guard bed to remove at least a portion of the colloidal or molecular catalyst from the upgraded feedstock produced by one or more slurry phase reactors before introducing it into one or more fixed bed reactors. This may be accomplished by selecting a guard bed catalyst that is able to scavenge the colloidal or molecular catalyst.

An upgraded fixed bed hydroprocessing system according to the invention may include processing and handling equipment upstream and downstream from the one or more fixed bed reactors as needed to yield a desired hydroprocessing system. Such other processing and handling equipment may include, for example, one or more of a preheating chamber, such as for causing the well dispersed catalyst precursor composition to decompose and/or for causing the heavy oil feedstock to liberate sulfur that can combine with the metal liberated from the catalyst precursor composition, a hot separator, a slurry phase reactor, a guard bed, an ebullated bed reactor, an atmospheric distillation tower, a vacuum distillation tower, a scrubber, an aqueous washing system, and conduits and channels for transporting the feedstock from one location in the system to another.

These and other advantages and features of the present invention will become more fully apparent from the following description and appended claims, or may be learned by the practice of the invention as set forth hereinafter.

BRIEF DESCRIPTION OF THE DRAWINGS

To further clarify the above and other advantages and features of the present invention, a more particular description of the invention will be rendered by reference to specific embodiments thereof which are illustrated in the appended drawings. It is appreciated that these drawings depict only typical embodiments of the invention and are therefore not to be considered limiting of its scope. The invention will be described and explained with additional specificity and detail through the use of the accompanying drawings, in which:

FIG. 1 depicts a hypothetical chemical structure for an asphaltene molecule;

FIG. 2A is a schematic diagram that illustrates an exemplary fixed bed reactor that may be incorporated into an improved fixed bed hydroprocessing system according to the invention;

FIG. 2B is a schematic diagram that illustrates an exemplary fixed bed hydroprocessing system comprising multiple fixed bed reactors that may be incorporated into, or upgraded to yield, an improved fixed bed hydroprocessing system according to the invention;

FIG. 3 is a flow diagram that schematically illustrates an exemplary process for preparing a heavy oil feedstock to include a molecular or colloidal catalyst dispersed therein;

FIG. 4 schematically illustrates catalyst molecules or colloidal-sized catalyst particles associated with asphaltene molecules;

FIGS. 5A and 5B schematically depict top and side views of a molybdenum disulfide crystal approximately 1 nm in size;

FIG. 6 is a schematic diagram of an exemplary fixed bed hydroprocessing system according to the invention that includes a slurry phase reactor, a hot separator, and a fixed bed reactor;

FIG. 7A-7C are block diagrams that illustrate exemplary fixed bed hydroprocessing systems according to the invention;

FIGS. 8A-8D are flow diagrams that illustrate exemplary methods for upgrading a pre-existing fixed bed hydroprocessing system;

FIG. 9 is a chart comparing the asphaltene conversions using a colloidal or molecular catalyst versus using a porous supported catalyst;

FIG. 10 is a schematic diagram of a pilot slurry phase/ebullated bed hydroprocessing system used to compare a colloidal or molecular catalyst according to the invention and a conventional ebullated bed catalyst;

FIG. 11 is a chart comparing increases in pressure drop across the second pilot ebullated bed reactor over time for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst;

FIG. 12 is a chart depicting resid conversion at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst;

FIG. 13 is a chart comparing asphaltene conversion at various hours on stream for test runs using either a porous supporting catalyst by itself or in combination with a colloidal or molecular catalyst;

FIG. 14 is a chart comparing desulfurization at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst;

FIG. 15 is a chart comparing increases in pressure drop across the second pilot ebullated bed reactor over time for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst;

FIG. 16 is a chart comparing resid conversion at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with the colloidal or molecular catalyst;

FIG. 17 is a chart comparing C₇ asphaltene conversion at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst.

FIG. 18 is a chart comparing hot separator bottom API gravity at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst.

FIG. 19 is a chart comparing unconverted resid API gravity at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst.

FIG. 20 is a chart comparing IP-375 sediment in hot separator bottoms at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst;

FIG. 21 is a chart comparing the asphaltene concentration in the hot separator bottoms at various hours on stream or test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst; and

FIG. 22 is a chart comparing the MCR in hot separator bottoms at various hours on stream for test runs using either a porous supported catalyst by itself or in combination with a colloidal or molecular catalyst.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

I. Introduction and Definitions

The present invention relates to fixed bed hydroprocessing methods and systems for improving the quality of a heavy oil feedstock. Such methods and systems employ a dual catalyst system that includes a molecularly- or colloidally-dispersed hydroprocessing catalyst and a porous supported catalyst, typically contained within separate reactors but alternatively within the same reactor(s). The fixed bed hydroprocessing methods and systems of the invention more effectively process asphaltene molecules, reduce or eliminate the formation of coke precursors and sediment, reduce equipment fouling, increase conversion levels, catalyze beneficial upgrading reactions that otherwise might not occur outside the pores of the supported catalyst used in conventional fixed bed reactors, and more efficiently use the porous supported catalyst.

The invention also relates to methods for upgrading a pre-existing fixed bed hydroprocessing system. This typically involves beginning to operate one or more slurry phase reactors employing the colloidal or molecular catalyst described herein upstream from one or more fixed bed reactors (e.g., by constructing one or more new slurry phase reactors and/or converting one or more fixed bed reactors into a slurry phase reactor).

The terms “colloidal catalyst” and “colloidally-dispersed catalyst” shall refer to catalyst particles having a particle size that is colloidal in size, e.g., less than about 100 nm in diameter, preferably less than about 10 nm in diameter, more preferably less than about 5 nm in diameter, and most preferably less than about 1 nm in diameter. The term “colloidal catalyst” includes, but is not limited to, molecular or molecularly-dispersed catalyst compounds.

The terms “molecular catalyst” and “molecularly-dispersed catalyst” shall refer to catalyst compounds that are essential “dissolved” or completely dissociated from other catalyst compounds or molecules in a heavy oil hydrocarbon feedstock, non-volatile liquid fraction, bottoms fraction, resid, or other feedstock or product in which the catalyst may be found. It shall also refer to very small catalyst particles that only contain a few catalyst molecules joined together (e.g., 15 molecules or less).

The terms “residual catalyst”, “residual molecular catalyst” and “residual colloidal catalyst” shall refer to catalyst molecules or colloidal particles that remain with an upgraded feedstock or material when transferred from one vessel to another (e.g., from a hydrocracking reactor to a hot separator, another hydroprocessing reactor, or distillation tower).

The term “conditioned feedstock” shall refer to a heavy oil feedstock into which an oil soluble catalyst precursor composition has been combined and mixed sufficiently so that, upon decomposition of the catalyst precursor and formation of the catalyst, the catalyst will comprise a colloidal or molecular catalyst dispersed within the feedstock.

The term “hydrocracking” shall refer to a process whose primary purpose is to reduce the boiling range of a heavy oil feedstock and in which a substantial portion of the feedstock is converted into products with boiling ranges lower than that of the original feedstock. Hydrocracking generally involves fragmentation of larger hydrocarbon molecules into smaller molecular fragments having a fewer number of carbon atoms and a higher hydrogen-to-carbon ratio. The mechanism by which hydrocracking occurs typically involves the formation of hydrocarbon free radicals during fragmentation followed by capping of the free radical ends or moieties with hydrogen. The hydrogen atoms or radicals that react with hydrocarbon free radicals during hydrocracking are generated at or by active catalyst sites.

The term “hydrotreating” shall refer to a more mild operation whose primary purpose is to remove impurities such as sulfur, nitrogen, oxygen, halides, and trace metals from the feedstock and saturate olefins and/or stabilize hydrocarbon free radicals by reacting them with hydrogen rather than allowing them to react with themselves. The primary purpose is not to change the boiling range of the feedstock. Hydrotreating is most often carried out using a fixed bed reactor, although other hydroprocessing reactors can also be used for hydrotreating, an example of which is an ebullated bed hydrotreater.

Of course, “hydrocracking” may also involve the removal of sulfur and nitrogen from a feedstock as well as olefin saturation and other reactions typically associated with “hydrotreating”. The terms “hydroprocessing” and “hydroconversion” shall broadly refer to both “hydrocracking” and “hydrotreating” processes, which define opposite ends of a spectrum, and everything in between along the spectrum.

The terms “solid supported catalyst”, “porous supported catalyst” and “supported catalyst” shall refer to catalysts that are typically used in conventional ebullated bed and fixed bed hydroprocessing systems, including catalysts designed primarily for hydrocracking or hydrodemetallization and catalysts designed primarily for hydrotreating. Such catalysts typically comprise (i) a catalyst support having a large surface area and numerous interconnected channels or pores of uneven diameter and (ii) fine particles of an active catalyst such as sulfides of cobalt, nickel, tungsten, and molybdenum dispersed within the pores. For example a heavy oil hydrocracking catalyst manufactured by Criterion Catalyst, Criterion 317 trilube catalyst, has a bi-modal pore size distribution, with 80% of the pores ranging between 30 to 300 Angstroms with a peak at 100 Angstroms and 20% of the pores ranging between 1000 to 7000 Angstroms with a peak at 4000 Angstroms. The pores for the solid catalyst support are of limited size due to the need for the supported catalyst to maintain mechanical integrity to prevent excessive breakdown and formation of excessive fines in the reactor. Supported catalysts are commonly produced as cylindrical pellets or spherical solids.

The term “heavy oil feedstock” shall refer to heavy crude, oils sands bitumen, bottom of the barrel and resid left over from refinery processes (e.g., visbreaker bottoms), and any other lower quality material that contains a substantial quantity of high boiling hydrocarbon fractions (e.g., that boil at or above 343° C. (650° F.), more particularly at or above about 524° C. (975° F.)), and/or that include a significant quantity of asphaltenes that can deactivate a solid supported catalyst and/or cause or result in the formation of coke precursors and sediment. Examples of heavy oil feedstocks include, but are not limited to, Lloydminster heavy oil, Cold Lake bitumen, Athabasca bitumen, atmospheric tower bottoms, vacuum tower bottoms, residuum (or “resid”), resid pitch, vacuum residue, and nonvolatile liquid fractions that remain after subjecting crude oil, bitumen from tar sands, liquefied coal, oil shale, or coal tar feedstocks to distillation, hot separation, and the like and that contain higher boiling fractions and/or asphaltenes.

The term “hydrocracking reactor” shall refer to any vessel in which hydrocracking (i.e., reducing the boiling range) of a feedstock in the presence of hydrogen and a hydrocracking catalyst is the primary purpose. Hydrocracking reactors are characterized as having an input port into which a heavy oil feedstock and hydrogen can be introduced, an output port from which an upgraded feedstock or material can be withdrawn, and sufficient thermal energy so as to form hydrocarbon free radicals in order to cause fragmentation of larger hydrocarbon molecules into smaller molecules. Examples of hydrocracking reactors include, but are not limited to, slurry phase reactors (i.e., a two phase, gas-liquid system), ebullated bed reactors (i.e., a three phase, gas-liquid-solid system), fixed bed reactors (i.e., a three-phase system that includes a liquid feed trickling downward over a fixed bed of solid supported catalyst with hydrogen typically flowing concurrently, but possibly countercurrently in some cases).

The term “hydrocracking temperature” shall refer to a minimum temperature required to effect significant hydrocracking of a heavy oil feedstock. In general, hydrocracking temperatures will preferably fall within a range of about 410° C. (770° F.) to about 460° C. (860° F.), more preferably in a range of about 420° C. (788° F.) to about 450° C. (842° F.), and most preferably in a range of about 430° C. (806° F.) to about 445° C. (833° F.). It will be appreciated that the temperature required to effect hydrocracking may vary depending on the properties and chemical make up of the heavy oil feedstock. Severity of hydrocracking may also be imparted by varying the space velocity of the feedstock, i.e., the residence time of feedstock in the reactor, while maintaining the reactor at a fixed temperature. Milder reactor temperature and longer feedstock space velocity are typically required for heavy oil feedstock with high reactivity and/or high concentration of asphaltenes.

The term “gas-liquid slurry phase hydrocracking reactor” shall refer to a hydroprocessing reactor that includes a continuous liquid phase and a gaseous disperse phase which forms a “slurry” of gaseous bubbles within the liquid phase. The liquid phase typically comprises a hydrocarbon feedstock that may contain a low concentration of a colloidal catalyst or molecular-sized catalyst, and the gaseous phase typically comprises hydrogen gas, hydrogen sulfide, and vaporized low boiling point hydrocarbon products. The term “gas-liquid-solid, 3-phase slurry hydrocracking reactor” is used when a solid catalyst is employed along with liquid and gas. The gas may contain hydrogen, hydrogen sulfide and vaporized low boiling hydrocarbon products. The term “slurry phase reactor” shall broadly refer to both type of reactors (e.g. those with a colloidal or molecular catalyst, those with a micron-sized or larger particulate catalyst, and those that include both). In most cases, it shall refer to a reactor that at least includes a colloidal or molecular catalyst. An exemplary slurry phase reactor is disclosed in U.S. application Ser. No. 10/225,937, filed Aug. 22, 2002, and entitled “APPARATUS FOR HYDROCRACKING AND/OR HYDROGENATING FOSSIL FUELS”, the disclosure of which is incorporated herein by specific reference.

The term “asphaltene” shall refer to the fraction of a heavy oil feedstock that is typically insoluble in paraffinic solvents such as propane, butane, pentane, hexane, and heptane and that includes sheets of condensed ring compounds held together by hetero oz g atoms such as sulfur, nitrogen; oxygen and metals. Asphaltenes broadly include a wide range of complex compounds having anywhere from 80 to 160,000 carbon atoms, with predominating molecular weights, as determined by solution techniques, in the 5000 to 10,000 range. About 80-90% of the metals in the crude oil are contained in the asphaltene fraction which, together with a higher concentration of non-metallic hetero atoms, renders the asphaltene molecules more hydrophilic and less hydrophobic than other hydrocarbons in crude. A hypothetical asphaltene molecule structure developed by A.G. Bridge and co-workers at Chevron is depicted in FIG. 1.

The terms “upgrade”, “upgrading” and “upgraded”, when used to describe a feedstock that is being or has been subjected to hydroprocessing, or a resulting material or product, shall refer to one or more of a reduction in the molecular weight of the feedstock, a reduction in the boiling point range of the feedstock, a reduction in the concentration of asphaltenes, a reduction in the concentration of hydrocarbon free radicals, and/or a reduction in the quantity of impurities, such as sulfur, nitrogen, oxygen, halides, and metals.

II. Fixed Bed Hydroprocessing Methods and System

A. Exemplary Fixed Bed Reactors and Systems

FIG. 2A schematically depicts an exemplary fixed bed reactor that is used to process a hydrocarbon feedstock and that can be part of a fixed bed hydroprocessing system that can be upgraded according to the invention. More particularly, FIG. 2A schematically depicts a conventional fixed bed reactor 10 that includes an input port 12 at the top of the fixed bed reactor 10 through which a heavy oil feedstock 14 and pressurized hydrogen gas 16 are introduced, and an output port 18 at the bottom of the fixed bed reactor 10 through which upgraded feedstock 20 is withdrawn.

The fixed bed reactor 10 further includes a plurality of vertically stacked and spaced apart catalyst beds 22 comprising a packed porous supported hydroprocessing catalyst 24. Above each catalyst bed 22 is a distributor grid 26, which helps to more evenly distribute the flow of feedstock 14 downward through the catalyst beds 22. Catalyst free zones 28 exist above and below each catalyst bed 22. Auxiliary ports 30 in the center and/or bottom of the fixed bed reactor 10 may be provided through which a cooling oil or hydrogen quench 32 can be introduced to cool heat generated by the hydroprocessing reactions, control the reaction rate, and thereby help prevent formation of coke precursors and sediment and/or excessive gas.

During operation, the supported catalyst 24 is never moved, replaced or regenerated. As a result, conventional fixed fed reactors such as fixed bed reactor 10 have progressively diminished conversion and/or require increased temperature and pressure to maintain a given conversion level. As will be discussed below, one way to prolong the life of a fixed bed reactor is to position a “guard bed” reactor upstream from a fixed bed reactor that, in essence, acts as a sacrificial reactor to remove as many of the impurities as possible that can foul the catalyst within the fixed bed reactor. The guard bed is shut down and regenerated with new catalyst much more frequently than downstream fixed bed reactors. Multiple guard beds may be provided in order for one guard bed to remain operational while another guard bed is shut down for regeneration via catalyst replacement.

FIG. 2B schematically depicts the EXXON RESIDfining system, identified as fixed bed hydroprocessing system 100, which is an example of a fixed bed hydroprocessing system that can be upgraded according to the invention. Other exemplary commercial fixed bed hydroprocessing systems include the Chevron RDS/VRDS Hydrotreating system, the Hyvahl system of Axens, and the Unicracking system of UOP and Unocal, each of which can be upgraded according to the invention. Fixed bed hydroprocessing system 110 includes three fixed bed reactors 110 in series for upgrading a heavy oil feedstock 114. The fuist fixed bed reactor 110 a is a guard bed that employs a demetalization catalyst to remove metals from the feedstock that might plug or otherwise cause fouling of the porous supported catalyst within downstream fixed bed reactors 110 b and 110 c.

The feedstock 114 is passed through a filter 118 and introduced into the top of guard bed reactor 110 a together with hydrogen gas 116 that is preliminary passed through a heater 120. The demetalized feedstock 122 a removed from the bottom of guard bed reactor 110 a is introduced into the top of first main fixed bed reactor 110 b, which is one of two main hydroprocessing reactors. The upgraded feedstock 122 b removed from the bottom of the first main fixed bed hydroprocessing reactor 110 b is introduced into the top of the second main fixed bed hydroprocessing reactor 110 c.

The upgraded feedstock 122 c from the second main fixed bed hydroprocessing reactor 110 c is sent to a high temperature separator 124 a, which separates the volatile and non-volatile fractions. The volatile fraction 126 a is then sent to a low temperature separator 124 b, which separates the gaseous and liquid fractions. The gaseous fraction 128 is introduced into a hydrogen sulfide absorber 130 to remove ammonia and yield hydrogen recycle gas 116 a, which is combined with makeup hydrogen 116 b to form hydrogen gas stream 116 that is combined with the feedstock and introduced into the guard bed 110 a, as described above.

The liquid fraction 132 a from the high temperature separator 124 a is combined with the liquid fraction 132 b from the low temperature separator 124 b to form a single liquid stream 132 that is introduced into a product fractionator 134. The produce fractionator separators the liquid stream 132 into various fractions, including fuel gas and naphtha, distillate, and desulfurized heavy oil.

B. Preparation and Characteristics of Colloidal or Molecular Catalyst

The inventive methods and systems for upgrading a heavy oil feedstock include the preliminary step of, or sub-system for, preparing a heavy oil feedstock so as to have a colloidal or molecular catalyst dispersed therein, an example of which is schematically illustrated in the flow diagram depicted in FIG. 3. According to one embodiment, an oil soluble catalyst precursor composition is pre-mixed with a diluent hydrocarbon stream to form a diluted precursor mixture. Preparing a heavy oil feedstock to include a colloidal or molecular catalyst also forms part of exemplary methods for upgrading a pre-existing fixed bed hydroprocessing system, as discussed more fully below.

The oil soluble catalyst precursor preferably has a decomposition temperature in ranige from about 100° C. (212° F.) to about 350° C. (662° F.), more preferably in a range of about 150° C. (302° F.) to about 300° C. (572° F.), and most preferably in a range of about 175° C. (347° F.) to about 250° C. (482° F.). Examples of exemplary catalyst precursor compositions include organometallic complexes or compounds, more specifically, oil soluble compounds or complexes of transition metals and organic acids. A currently preferred catalyst precursor is molybdenum 2-ethylhexanoate (also commonly known as molybdenum octoate) containing 15% by weight molybdenum and having a decomposition temperature or range high enough to avoid substantial decomposition when mixed with a heavy oil feedstock at a temperature below about 250° C. (482° F.). Other exemplary precursor compositions include, but are not limited to, molybdenum naphthanate, vanadium naphthanate, vanadium octoate, molybdenum hexacarbonyl, vanadium hexacarbonyl, and iron pentacarbonyl. One of skill in the art can, following the present disclosure, select a mixing temperature profile that results in intimate mixing of a selected precursor composition without substantial decomposition prior to formation of the colloidal or molecular catalyst.

Examples of suitable hydrocarbon diluents include, but are not limited to, vacuum gas oil (which typically has a boiling range of 360-524° C.) (680-975° F.), decant oil or cycled oil (which typically has a boiling range of 360′-550° C.) (680-1022° F.), and light gas oil (which typically has a boiling range of 200°-360° C.) (392-680° F.).

The ratio of catalyst precursor composition to hydrocarbon oil diluent is preferably in a range of about 1:500 to about 1:1, more preferably in a range of about 1:150 to about 1:2, and most preferably in a range of about 1:100 to about 1:5 (e.g., 1:100, 1:50, 1:30, or 1:10).

The catalyst precursor composition is advantageously mixed with the hydrocarbon diluent at a temperature below which a significant portion of the catalyst precursor composition starts to decompose, preferably, at temperature in a range of about 25° C. (77° F.) to about 250° C. (482° F.), more preferably in range of about 50° C. (122° F.) to about 200° C. (392° F.), and most preferably in a range of about 750° C. (167° F.) to about 150° C. (302° F.), to form the diluted precursor mixture. It will be appreciated that the actual temperature at which the diluted precursor mixture is formed typically depends largely on the decomposition temperature of the particular precursor composition that is utilized. The precursor composition is preferably mixed with the hydrocarbon oil diluent for a time period in a range of about 1 second to about 20 minutes, more preferably in a range of about 5 seconds to about 10 minutes, and most preferably in a range of about 20 seconds to about 5 minutes. The actual mixing time is dependent, at least in part, on the temperature (i.e., which affects the viscosity of the fluids) and mixing intensity. Mixing intensity is dependent, at least in part, on the number of stages e.g., for in-line static mixer.

Whereas it is within the scope of the invention to directly blend the catalyst precursor composition with the heavy oil feedstock, care must be taken in such cases to mix the components for a time sufficient to thoroughly blend the precursor composition within the feedstock before substantial decomposition of the precursor composition has occurred. For example, U.S. Pat. No. 5,578,197 to Cyr et al., the disclosure of which is incorporated by reference, describes a method whereby molybdenum 2-ethyl hexanoate was mixed with bitumen vacuum tower residuum for 24 hours before the resulting mixture was heated in a reaction vessel to form the catalyst compound and to effect hydrocracking (see col. 10, lines 4-43). Whereas 24-hour mixing in a testing environment may be entirely acceptable, such long mixing times may make certain industrial operations prohibitively expensive.

It has now been found that preblending the precursor composition with a hydrocarbon diluent prior to blending the diluted precursor mixture with the heavy oil feedstock greatly aids in thoroughly and intimately blending the precursor composition within the feedstock, particularly in the relatively short period of time required for large-scale industrial operations to be economically viable. Forming a diluted precursor mixture shortens the overall mixing time by (1) reducing or eliminating differences in solubility between the more polar catalyst precursor composition and the heavy oil feedstock, (2) reducing or eliminating differences in rheology between the catalyst precursor composition and the heavy oil feedstock, and/or (3) breaking up the catalyst precursor molecules to form a solute within a hydrocarbon oil diluent that is much more easily dispersed within the heavy oil feedstock. It is particularly advantageous to first form a diluted precursor mixture in the case where the heavy oil feedstock contains water (e.g., condensed water). Otherwise, the greater affinity of the water for the polar catalyst precursor composition can cause localized agglomeration of the precursor composition, resulting in poor dispersion and formation of micron-sized or larger catalyst particles. The hydrocarbon oil diluent is preferably substantially water free (i.e., contains less than about 0.5% water) to prevent the formation of substantial quantities of micron-sized or larger catalyst particles.

The diluted precursor mixture is then combined with the heavy oil feedstock and mixed for a time sufficient and in a manner so as to disperse the catalyst precursor composition throughout the feedstock in order to yield a conditioned feedstock composition in which the precursor composition is thoroughly mixed within the heavy oil feedstock. In order to obtain sufficient mixing of the catalyst precursor composition within the heavy oil feedstock so as to yield a colloidal or molecular catalyst upon decomposition of the precursor composition, the diluted precursor mixture and heavy oil feedstock are preferably mixed for a time period in a range of about 1 second to about 20 minutes, more preferably in a range from about 5 second to about 10 minutes, and most preferably in a range of about 20 seconds to about 3 minutes. Increasing the vigorousness and/or shearing energy of the mixing process generally reduce the time required to effect thorough mixing.

Examples of mixing apparatus that can be used to effect thorough mixing of the catalyst precursor composition and heavy oil feedstock include, but are not limited to, high shear mixing such as mixing created in a vessel with a propeller or turbine impeller; multiple static in-line mixers; multiple static in-line mixers in combination with in-line high shear mixers; multiple static in-line mixers in combination with in-line high shear mixers; multiple static in-line mixers in combination with in-line high shear mixers follows by a pump around in the surge vessel; combinations of the above followed by one or more multi-stage centrifugal pumps; and one or more multi-stage centrifugal pumps. According to one embodiment, continuous rather than batch-wise mixing can be carried out using high energy pumps having multiple chambers within which the catalyst precursor composition and heavy oil feedstock are churned and mixed as part of the pumping process itself. The foregoing mixing apparatus may also be used for the pre-mixing process discussed above in which the catalyst precursor composition is mixed with the hydrocarbon oil diluent to form the catalyst precursor mixture.

Alternatively, the diluted precursor mixture can be initially mixed with 20% of the heavy oil feedstock, the resulting mixed heavy oil feedstock can be mixed in with another 40% of the heavy oil feedstock, and the resulting 60% of the mixed heavy oil feedstock can be mixed in with the remainder 40% of heavy oil in accordance with good engineering practice of progressive dilution to thoroughly dispersed the catalyst precursor in the heavy oil feedstock. Vigorous adherence to the mixing time in the appropriate mixing devices or methods described herein should still be used in the progressive dilution approach.

In the case of heavy oil feedstocks that are solid or extremely viscous at room temperature, such feedstocks may advantageously be heated in order to soften them and create a feedstock having sufficiently low viscosity so as to allow good mixing of the oil soluble catalyst precursor into the feedstock composition. In general, decreasing the viscosity of the heavy oil feedstock will reduce the time required to effect thorough and intimate mixing of the oil soluble precursor composition within the feedstock. However, the feedstock should not be heated to a temperature above which significant decomposition of the catalyst precursor composition occurs until after thorough and complete mixing to form the blended feedstock composition. Prematurely decomposing the catalyst precursor composition generally results in the formation of micron-sized or larger catalyst particles rather than a colloidal or molecular catalyst. The heavy oil feedstock and diluted precursor mixture are preferably mixed and conditioned at a temperature in a range of about 25° C. (77° F.) to about 350° C. (662° F.), more preferably in a range of about 50° C. (122° F.) to about 300° C. (572° F.), and most preferably in a range of about 75° C. (167° F.) to about 250° C. (482° F.) to yield the conditioned feedstock.

After the catalyst precursor composition has been well-mixed throughout the heavy oil feedstock so as to yield the conditioned feedstock composition, this composition is then heated to above the temperature where significant decomposition of the catalyst precursor composition occurs in order to liberate the catalyst metal therefrom so as to form the final active catalyst. According to one embodiment, the metal from the precursor composition is believed to first form a metal oxide, which then reacts with sulfur liberated from the heavy oil feedstock to yield a metal sulfide compound that is the final active catalyst. In the case where the heavy oil feedstock includes sufficient or excess sulfur, the final activated catalyst may be formed in situ by heating the heavy oil feedstock to a temperature sufficient to liberate the sulfur therefrom. In some cases, sulfur may be liberated at the same temperature that the precursor composition decomposes. In other cases, further heating to a higher temperature may be required.

If the oil soluble catalyst precursor composition is thoroughly mixed throughout the heavy oil feedstock, at least a substantial portion of the liberated metal ions will be sufficiently sheltered or shielded from other metal ions so that they can form a molecularly-dispersed catalyst upon reacting with sulfur to form the metal sulfide compound. Under some circumstances, minor agglomeration may occur, yielding colloidal-sized catalyst particles. However, it is believed that taking care to thoroughly mix the precursor composition throughout the feedstock will yield individual catalyst molecules rather than colloidal particles. Simply blending, while failing to sufficiently mix, the catalyst precursor composition with the feedstock typically causes formation of large agglomerated metal sulfide compounds that are micron-sized or larger.

In order to form the metal sulfide catalyst, the blended feedstock composition is preferably heated to a temperature in a range of about 275° C. (527° F.) to about 450° C. (842° F.), more preferably in a range of about 350° C. (662° F.) to about 440° C. (824° F.), and most preferably in a range of about 375° C. (707° F.) to about 420° C. (788° F.). According to one embodiment, the conditioned feedstock is heated to a temperature that is about 100° C. (180° F.) less than the hydrocracking temperature within the hydrocracking reactor, preferably about 50° C. (90° F.) less than the hydrocracking temperature. According to one embodiment, the colloidal or molecular catalyst is formed during preheating before the heavy oil feedstock is introduced into the hydrocracking reactor. According to another embodiment, at least a portion of the colloidal or molecular catalyst is formed in situ within the hydrocracking reactor itself. In some cases, the colloidal or molecular catalyst can be formed as the heavy oil feedstock is heated to a hydrocracking temperature prior to or after the heavy oil feedstock is introduced into a hydrocracking reactor. The initial concentration of the catalyst metal in the colloidal or molecular catalyst is preferably in a range of about 5 ppm to about 500 ppm by weight of the heavy oil feedstock, more preferably in a range of about 15 ppm to about 300 ppm, and most preferably in a range of about 25 ppm to about 175 ppm. The catalyst may become more concentrated as volatile fractions are removed from a non-volatile resid fraction.

In the case where the heavy oil feedstock includes a significant quantity of asphaltene molecules, the catalyst molecules or colloidal particles will preferentially associate with, or remain in close proximity to, the asphaltene molecules. Asphaltene has a greater affinity for the colloidal or molecular catalyst since asphaltene molecules are generally more hydrophilic and less hydrophobic than other hydrocarbons contained within the heavy oil feedstock. Because the colloidal or molecular catalyst tends to be very hydrophilic, the individual particles or molecules will tend to migrate toward the more hydrophilic moieties or molecules within the heavy oil feedstock. FIG. 4 schematically depicts catalyst molecules, or colloidal particles “X” associated with or in close proximity to, the asphaltene molecules.

While the highly polar nature of the catalyst compound causes or allows the colloidal or the molecular catalyst to associate with asphaltene molecules, it is the general incompatibility between the highly polar catalyst compound and the hydrophobic heavy oil feedstock that necessitates the aforementioned intimate or thorough mixing of the oil soluble catalyst precursor composition within the heavy oil feedstock prior to decomposition of the precursor and formation of the colloidal or molecular catalyst. Because metal catalyst compounds are highly polar, they cannot be effectively dispersed within a heavy oil feedstock in colloidal or molecular form if added directly thereto or as part of an aqueous solution or an oil and water emulsion. Such methods inevitably yield micron-sized or larger catalyst particles.

Reference is now made to FIGS. 5A and 5B, which schematically depict a nanometer-sized molybdenum disulfide crystal. FIG. 5A is a top view, and FIG. 5B is a side view, of a molybdenum disulfide crystal. Molecules of molybdenum disulfide typically form flat, hexagonal crystals in which single layers of molybdenum (Mo) atoms are sandwiched between layers of sulfur (S) atoms. The only active sites for catalysis are on the crystal edges where the molybdenum atoms are exposed. Smaller crystals have a higher percentage of molybdenum atoms exposed at the edges.

The diameter of a molybdenum atom is approximately 0.3 nm, and the diameter of a sulfur atom is approximately 0.2 nm. A nanometer-sized crystal of molybdenum disulfide has 7 molybdenum atoms sandwiched in between 14 sulfur atoms. As best seen in FIG. 6A, 6 out of 7 (85.7%) of the total molybdenum atoms will be exposed at the edge and available for catalytic activity. In contrast, a micron-sized crystal of molybdenum disulfide has several million atoms, with only about 0.2% of the total molybdenum atoms being exposed at the crystal edge and available for catalytic activity. The remaining 99.8% of the molybdenum atoms in the micron-sized crystal are embedded within the crystal interior and are therefore unavailable for catalysis. This means that nanometer-sized molybdenum disulfide particles are, at least in theory, orders of magnitude more efficient than micron-sized particles in providing active catalyst sites.

In practical terms, forming smaller catalyst particles results in more catalyst particles and more evenly distributed catalyst sites throughout the feedstock. Simple mathematics dictates that forming nanometer-sized particles instead of micron-sized particles will result in approximately 1000³ (or 1 million) to 1000³ (or 1 billion) times more particles depending on the size and shape of the catalyst crystals. That means there are approximately 1 million to 1 billion times more points or locations within the feedstock where active catalyst sites reside. Moreover, nanometer-sized or smaller molybdenum disulfide particles are believed to become intimately associated with asphaltene molecules, as shown in FIG. 4. In contrast, micron-sized or larger catalyst particles would be far too large to become intimately associated with or within asphaltene molecules.

C. Fixed Bed Reactors and Systems that Employ the Colloidal or Molecular Catalyst

FIG. 6 schematically illustrates an exemplary fixed bed hydroprocessing system 400 according to the invention. Fixed bed hydroprocessing system 400 includes a slurry phase hydrocracking reactor 402, a hot separator 404, and a fixed bed reactor 460 downstream from the hot separator 404. A heavy oil feedstock 406 is initially blended and conditioned with a catalyst precursor composition 408 within a mixer 410, preferably after first pre-mixing the precursor composition 408 with a diluent as discussed above. The conditioned feedstock from the mixer 410 is pressurized by a pump 412, passed through a pre-heater 413, and continuously or periodically fed into the slurry phase reactor 402 together with hydrogen gas 414 through an input port 418 located at or near the bottom of the slurry phase reactor 402. A recycle channel 419, recycle pump 420, and distributor grid plate 421 with bubble caps at the bottom of the slurry phase reactor 402 helps to more evenly disperse the hydrogen 414, schematically depicted as gas bubbles 422, within the feedstock 406. The colloidal or molecular catalyst within the feedstock 406 is schematically depicted as catalyst particles 424. It will be appreciated that gas bubbles 422 and catalyst particles 424 are shown oversized so that they may be seen in the drawing. In reality, they are likely invisible to the naked eye.

The heavy oil feedstock 406 is catalytically upgraded in the presence of the hydrogen and colloidal or molecular catalyst within the slurry phase reactor 402 to form an upgraded feedstock 426, which is continuously or periodically withdrawn from the slurry phase reactor 402 through an output port 428 located at or near the top of the slurry phase reactor 402 and introduced into a hot separator 404. The upgraded feedstock 426 contains residual or molecular catalyst, schematically depicted as catalyst particles 424′ within the hot separator 404.

The hot separator 404 separates the volatile faction 405, which is withdrawn from the top of hot separator 404, from the non-volatile fraction 407, which is withdrawn from the bottom of hot separator 404. According to one embodiment, the hot separator is advantageously operated at a temperature within about 20° F. (about 11° C.) of the hydroprocessing temperature within the fixed bed reactor 430. The non-volatile fraction 407 still contains residual colloidal or molecular catalyst 424′ and residual hydrogen gas (schematically depicted as bubbles 4221 dispersed therein. As a result, beneficial hydrogenation reactions between hydrocarbon free radicals that still exist or that are formed within the non-volatile faction 407 and the residual hydrogen 422′ can be catalyzed by the residual colloidal or molecular catalyst 424′ within the hot separator 404. There is therefore no need to add quenching oil to the further upgraded feedstock 426 to prevent fouling of the hot separator 404.

The non-volatile fraction 407 is then introduced into the fixed bed reactor 460, either directly or after optionally passing the non-volatile fraction 407 through optionally hydroprocessing apparatus. The fixed bed reactor 460 may be designed to perform hydrocracking and/or hydrotreating reactions depending on the operating temperature and/or the type of solid supported catalyst that is used within the fixed bed reactor 460. Fixed bed reactor 460 more particularly includes an input port 462 at the top of the through which the non-volatile fraction 407 and supplemental hydrogen gas 464 are introduced, and an output port 466 at the bottom through which a further hydroprocessed feedstock 468 is withdrawn. The fixed bed reactor 460 further includes a plurality of vertically stacked and spaced apart catalyst beds 470 comprising a packed porous supported catalyst. Above each catalyst bed 470 is a distributor grid 472, which helps to more evenly distribute the flow of feedstock downward through the catalyst beds 470. Supported catalyst free zones 474 exist above and below each catalyst bed 470. To the extent the residual colloidal or molecular catalyst 424′ is not preliminarily removed by a guard bed it remains dispersed throughout the feedstock within the fixed bed reactor 460, including the catalyst beds 470 and the zones 474 above and below the catalyst beds 470, thereby being available to promote upgrading reactions outside the pores of the fixed bed catalyst. Auxiliary ports 476 in the center and/or bottom of the fixed bed reactor 460 may be provided through which a cooling oil and/or hydrogen quench can be introduced to cool heat generated by the hydroprocessing reactions, control the reaction rate, and thereby help prevent formation of coke precursors and sediment and/or excessive gas within the fixed bed reactor 460.

FIGS. 7A-7C further illustrate exemplary fixed bed hydroprocessing systems according to the invention, including upgraded systems from pre-existing fixed bed systems. FIG. 7A is a box diagram that schematically illustrates an exemplary hydroprocessing system 500 which includes a fixed bed reactor 502 that differs from a conventional fixed bed system by blending a catalyst precursor composition 504 with a heavy oil feedstock 506 prior to introducing the feedstock 506 into the fixed bed reactor 502 and downstream apparatus 508. Downstream apparatus 508 may comprise one or more additional fixed bed reactors, other hydrocracking or hydroprocessing reactors, hot separators, distillation towers, a guard bed, and the like.

The heavy oil feedstock 506 may comprise any desired fossil fuel feedstock and/or fraction thereof including, but not limited to, one or more of heavy crude, oil sands bitumen, bottom of the barrel fractions from crude oil, atmospheric tower bottoms, vacuum tower bottoms, coal tar, liquefied coal, and other resid fractions. According to one embodiment, the heavy oil feedstock 506 includes a significant fraction of high boiling point hydrocarbons (i.e., at or above 343° C. (650° F.), more particularly at or above about 524° C. (975° F.)) and/or asphaltenes. Asphaltenes are complex hydrocarbon molecules that include a relatively low ratio of hydrogen to carbon that is the result of a substantial number of condensed aromatic and naphthenic rings with paraffinic side chains (See FIG. 1). Sheets consisting of the condensed aromatic and naphthenic rings are held together by heteroatoms such as sulfur or nitrogen and/or polymethylene bridges, thio-ether bonds, and vanadium and nickel complexes. The asphaltene fraction also contains a higher content of sulfur and nitrogen than does crude oil or the rest of the vacuum resid, and it also contains higher concentrations of carbon-forming compounds (i.e., that form coke precursors and sediment).

The catalyst precursor composition 504 is intimately mixed with the feedstock 506 prior to introducing the feedstock into the fixed bed reactor 502. According to one embodiment, the catalyst precursor composition may be pre-mixed with a diluent hydrocarbon stream (not shown) to form a diluted precursor mixture that is then mixed with the heavy oil feedstock 506. The colloidal or molecular catalyst may be generated prior to introducing the feedstock 506 into the fixed bed reactor 502 and/or generated in situ within the fixed bed reactor 402. In this way, the fixed bed reactor 502 within hydroprocessing system 500 employs a colloidal or molecular catalyst, which provides the benefits described above (e.g., promotes beneficial upgrading reactions involving asphaltenes or other large hydrocarbon molecules that are too large to diffuse into the pores of a porous supported catalyst and provides a hydroprocessing catalyst in what would otherwise constitute catalyst free zones inherent in a fixed bed reactor and downstream apparatus 508).

FIG. 7B is a box diagram that schematically illustrates an exemplary fixed bed hydroprocessing system 600 that includes a slurry phase reactor 610 upstream from a fixed bed reactor 602 and downstream apparatus 608. The slurry phase reactor 610 may comprise a previously operating fixed bed reactor that has been converted into a slurry phase reactor, or it may comprise a newly constructed reactor within the hydroprocessing system 600. The catalyst precursor composition 604 is intimately mixed with the heavy oil feedstock 606 prior to introducing the feedstock 606 into the slurry phase reactor 610. The slurry phase reactor 610 yields an upgraded feedstock, which is thereafter introduced into the fixed bed reactor 602, either directly or after additional processing (e.g., one or more additional slurry phase reactors, one or more hot separators, and/or one or more fixed bed reactors upstream from fixed bed reactor 602). The hydroprocessing system 600 may further include downstream apparatus 608 as desired to complete the system (e.g., one or more of a guard bed, fixed bed hydrotreating reactor, hot separator, and the like).

FIG. 8C is a box diagram that schematically illustrates an exemplary fixed bed hydroprocessing system 700 that includes a slurry phase reactor 710 and a guard bed 712 upstream from a fixed bed reactor 712. The catalyst precursor composition 704 is intimately mixed with the heavy oil feedstock 706 prior to introducing the feedstock 706 into the slurry phase reactor 710. The slurry phase reactor 710 yields an upgraded feedstock, which is thereafter introduced into the guard bed 712 in order to remove impurities that might otherwise shorten the life of the porous supported catalyst or otherwise foul the fixed bed reactor 702. The guard bed 712 advantageously comprises a fixed bed reactor that includes a catalyst that is specially designed to remove targeted impurities (e.g., one or more of metal impurities such as nickel and vanadium and at least a portion of the colloidal or molecular catalyst). The hydroprocessing system 700 may further include downstream apparatus 708 as desired to complete the system.

Any of the foregoing exemplary fixed bed hydroprocessing systems, as well as others, that may be made by those of skill in the art based on the teachings disclosed herein, may comprise entirely new equipment (e.g., a “green field operation”), or they may integrate one or more components from pre-existing hydroprocessing systems. It is within the scope of the invention to upgrade a pre-existing fixed bed reactor or hydroprocessing system to yield a hydroprocessing system according to the invention.

D). Methods for Upgrading an Existing Fixed Bed Reactor or System

FIGS. 8A-8D show box diagrams that schematically illustrate exemplary methods for upgrading pre-existing fixed bed reactors and systems according to the invention. FIG. 8A is a box diagram of an exemplary method 800 for upgrading a pre-existing fixed bed reactor. The first step or act involves operating a pre-existing fixed bed hydroprocessing system comprising one or more fixed bed reactors, each of which employs one or more packed beds of a porous supported catalyst (e.g., 1-3). Such catalysts typically have a size of, for example, ¼″×⅛″ or ¼″× 1/16″ (6.35 mm×3.175 mm or 6.35 mm×1.5875 mm), and include a porous support material and metal catalyst sites disposed within the pores of the support material As discussed above, the heavy oil feedstock molecules, more particularly the hydrocarbon free radicals generated by thermal cracking, must diffuse into the pores of the catalyst. As a result, larger molecules such as asphaltenes that are too large to enter the pores cannot be effectively hydroprocessed using the porous supported catalyst. Moreover, hydrocarbon free radicals of any size outside the pores of the porous supported catalyst of the fixed bed reactor cannot be hydroprocessed because they are not in contact with the metal catalyst particles.

The fixed bed hydroprocessing system in this method is upgraded by operating one or more fixed bed using a colloidal or molecular catalyst in addition to the porous supported catalyst. The colloidal or molecular catalyst can be generated within a heavy oil feedstock prior to introducing the feedstock into the fixed bed reactor, or the feedstock may contain a well-dispersed catalyst precursor composition that forms the colloidal or molecular catalyst in situ within a fixed bed reactor. Exemplary methods for preparing the colloidal or molecular catalyst within a feedstock are described more fully above. In this embodiment it will be advantageous to utilize a porous supported catalyst that is designed so as to not remove a substantial portion of the colloidal or molecular catalyst from the heavy oil feedstock.

Operating the fixed bed reactor using the colloidal or molecular catalyst immediately helps to offset at least two deficiencies inherent in the pre-existing fixed bed hydroprocessing system prior to upgrading according to the invention. First, the colloidal or molecular catalyst remains within the heavy oil feedstock as it passes through zones above and below the catalyst beds prior to upgrading. As a result, the colloidal or molecular catalyst catalyzes beneficial upgrading reactions of the feedstock throughout the entire reaction chamber, not just within the packed catalyst beds comprising the supported catalyst. Free radicals formed anywhere in the reaction chamber, and even within downstream processing equipment (e.g., hot separators), can be capped with hydrogen wherever the colloidal or molecular catalyst exists within the feedstock. Second, asphaltenes and other hydrocarbon molecules that are too large to enter the pores of the supported catalyst, as well as hydrocarbon molecules that otherwise fail to diffuse into the pores of the fixed bed catalyst, can be hydroprocessed by the colloidal or molecular catalyst. The use of the colloidal or molecular catalyst increases the conversion levels of the feedstock, decreases fouling of the fixed bed reactor(s) and/or other processing equipment, and extends the life of the porous supported catalyst.

FIG. 8B is a box diagram of an exemplary method 802 for upgrading a pre-existing fixed bed hydroprocessing system comprising multiple fixed bed reactors. It should be understood that operating and upgrading a fixed bed hydroprocessing system comprising multiple fixed bed reactors as illustrated in FIG. 8B is not mutually exclusive to operating and upgrading a fixed bed hydroprocessing system as described above with respect to FIG. 8A. The first step or act involves operating a pre-existing fixed bed hydroprocessing system comprising multiple fixed bed reactors using a porous supported catalyst within each reactor. The fixed bed hydroprocessing system is upgraded by introducing a colloidal or molecular catalyst into one or more of the fixed bed reactors. According to one embodiment, each of the fixed bed reactors upstream from any guard bed(s) in the upgraded hydroprocessing system employs both a porous supported catalyst and the colloidal or molecular catalyst.

According to another embodiment, the fixed bed hydroprocessing system is also modified by eliminating at least a portion of the porous supported catalyst from at least one of the fixed bed reactors. Eliminating all of the porous supported catalyst from a particular fixed bed reactor and using the colloidal or molecular catalyst in its place effectively converts it into a “slurry phase reactor”, as that term has been defined herein. Operating a slurry phase reactor upstream from one or more fixed bed reactors allows for beneficial upgrading of the feedstock by the colloidal or molecular catalyst prior to introducing the upgraded into one or more fixed bed reactors. This is particularly beneficial in the case where the feedstock initially includes a relatively high quantity of asphaltenes (e.g., greater than 10%) or other large hydrocarbon molecules that are too large to enter the pores of the fixed bed catalyst. The colloidal or molecular catalyst within the slurry phase reactor advantageously breaks down a substantial portion of the asphaltenes and/or other large hydrocarbon molecules into smaller molecules that are better able to diffuse into the pores of the supported catalyst used in one or more fixed bed reactors downstream form the slurry phase reactor. The result is increased conversion of the feedstock, reduced equipment fouling, and increased life of the supported catalyst.

FIG. 8C is a box diagram of an exemplary method 804 for upgrading a pre-existing fixed bed hydroprocessing system comprising at least one fixed bed reactor. It should be understood that operating and upgrading at least one fixed bed reactor as illustrated in FIG. 5C is not mutually exclusive to operating and upgrading a fixed bed reactor according to FIG. 8A or fixed bed hydroprocessing system as described relative to FIG. 8B. The first step or act involves operating a pre-existing fixed bed hydroprocessing system comprising at least one fixed bed reactor using a porous supported catalyst.

The fixed bed hydroprocessing system is upgraded by operating one or more slurry phase reactors using a colloidal or molecular catalyst upstream from the one or more fixed bed reactors of the pre-existing fixed bed hydroprocessing system. This may be accomplished by constructing one or more new slurry phase reactors upstream from one or more pre-existing fixed bed reactors, which is similar in effect to converting a pre-existing fixed bed reactor into a slurry phase reactor according to one of the embodiments of the method of FIG. 8B. One benefit of constructing one or more new slurry phase reactors upstream from the pre-existing fixed bed reactors is that it permits maintaining the same number of fixed bed reactors as previously existed within the pre-existing fixed bed hydroprocessing system. It also allows one to design and tailor the one or more slurry phase reactors to desired specifications. It is within the scope of the invention for an upgraded fixed bed hydroprocessing system to include both a newly built slurry phase reactor and one that has been converted from a fixed bed reactor.

FIG. 8D is a box diagram of an exemplary method 806 for upgrading a pre-existing fixed bed hydroprocessing system comprising one or more fixed bed reactors in a manner that is expressly designed to prolong the life of the supported catalyst within one or fixed bed reactors downstream from a slurry phase reactor. It should be understood that operating and upgrading a fixed bed hydroprocessing system as illustrated in FIG. 5D is not mutually exclusive to operating and upgrading one or more fixed bed reactors as described above with respect to FIGS. 8A-8C. The first step or act involves operating a pre-existing fixed bed hydroprocessing system comprising at least one fixed bed reactor using a porous supported catalyst.

As in the examples relating to FIGS. 8B and 8C, the fixed bed hydroprocessing system is initially upgraded by beginning operating one or more slurry phase reactors using a colloidal or molecular catalyst upstream from at least one fixed bed reactor. After upgrading the feedstock in the one or more slurry phase reactors, the upgraded feedstock is first passed through a guard bed in order to at least remove metal impurities prior to introducing the cleaned feedstock into one or more fixed bed reactors. The guard bed may be designed to remove at least a portion of the colloidal or molecular catalyst from the feedstock prior to introducing the feedstock into one or fixed bed reactors downstream from the guard bed.

As compared to conventional fixed bed hydroprocessing methods, which are only capable of conversion levels of about 25% or less, the improved fixed bed hydroprocessing methods and systems of the present invention preferably achieve conversion levels of at least about 50%, more preferably at least about 65%, and most preferably at least about 80%. Use of the colloidal or molecular catalyst can achieve conversion levels up to about 95%. Moreover, whereas conventional fixed bed systems typically have a lower conversion level for the asphaltene fraction as compared to the heavy oil feedstock as a whole, the improved fixed bed hydroprocessing methods and systems preferably maintain similar conversion levels for both the asphaltene fraction and the overall heavy oil feedstock.

III. Experimental Studies and Results

The following test studies demonstrate the effects and advantages of using a colloidal or molecular catalyst instead of, and in addition to, a conventional porous supported catalyst when hydroprocessing a heavy oil feedstock that includes a significant quantity of asphaltenes.

EXAMPLE 1

The ability of a colloidal or molecular catalyst and a porous supported catalyst to convert the asphaltene fraction of a heavy oil feedstock was compared. A heavy oil feedstock comprising Cold Lake bitumen atmospheric resid and 300 ppm of a molybdenum disulfide catalyst in colloidal or molecular form was introduced into a pilot slurry phase hydroprocessing reactor system and operated at various percent resid conversion levels. The pilot reactor system used in this test was similar to that shown in FIG. 10 (discussed more fully below), except that the pilot reactor system only had a single continuous flow slurry phase reactor having a volume of 1200 ml. The pilot reactor was a hollow tube and had no internal liquid recycle system. The pilot plant experiments were carried out under 2000 psig of hydrogen pressure, with a reaction temperature over the range of 430450° C. to control the conversion level and a hydrogen flow rate of 5000 standard cubic feet per barrel of heavy oil (SCF/bbl). The percent conversion of the asphaltenes versus the overall conversion level for the resid material when using the colloidal or molecular catalyst is plotted in the chart shown at FIG. 9.

Cold Lake bitumen atmospheric resid was also hydroprocessed using a porous supported catalyst within a 3 phase, gas-liquid-solid continuous flow stirred reactor that was operated at various percent resid conversion levels. The porous supported catalyst was contained within a spinning cage and experiments were carried out at 2000 psig hydrogen pressure at reaction temperature between 420-440° C. to control the conversion level. The percent conversion of the asphaltenes versus the overall conversion level for the resid material when using the porous supported catalyst is also plotted in the chart shown at FIG. 9.

According to the chart of FIG. 9, the comparative study showed that the percent conversion of asphaltenes using the colloidal or molecular catalyst was the same as the percent conversion of the resid material as a whole. That means the asphaltenes were converted into lower boiling materials at the same conversion level as the resid material as a whole, demonstrating that the colloidal or molecular catalyst was as active in converting asphaltenes as other resid hydrocarbon molecules. In practical terms, the result is no incremental buildup of asphaltenes in the feedstock.

In contrast, the percent conversion of asphaltenes using the porous supported catalyst was half or less of the percent conversion of the resid fraction as a whole. That means the porous supported catalyst was substantially less effective in converting asphaltenes than other hydrocarbons in the resid material, most likely because the larger asphaltenes are not able to diffuse into the pores of catalyst as readily as other, smaller molecules in the resid material. As a result, a much higher proportion of asphaltenes remained unconverted, and the remaining unconverted resid material contained an increased proportion of asphaltenes. Producing a resid material having an ever-increasing concentration of asphaltenes would be expected to lead to catalyst and equipment fouling, which is why only diluted vacuum tower residuum or low asphaltene feedstocks can be hydroprocessed using conventional ebullated bed and fixed bed systems and at a conversion level less than 60.

EXAMPLE 2

A heavy oil feedstock comprising Athabasca vacuum tower bottoms (which included 21 wt. % of pentane insoluble asphaltenes) from the Syncrude Canada Ltd. plant in Alberta, Canada, with 150 ppm of a molybdenum sulfide catalyst in colloidal or molecular form was introduced into a pilot plant similar to the one shown in FIG. 10 having two gas-liquid slurry phase reactors connected in series. Each reactor had a volume of 2200 ml. The first reactor was heated to a weighted averaged temperature below 370° C. (698° F.), and the second reactor was heated to a weighted averaged temperature between 419-445° C. (786-833° F.) and liquid hourly space velocity between 0.41 and 0.7/hr. The results of this test showed that the concentration of the asphaltene in the residual resid at 75% conversion was also 21 wt. %, which was identical to that in the original feedstock, thereby further confirming the ability of the colloidal or molecular catalyst to convert the asphaltene fraction at the same rate as the resid material as a whole.

EXAMPLE 3

This example tested the ability of a colloidal or molecular catalyst utilized in a slurry phase reactor according to the invention to convert various resid materials and their asphaltene and sulfur fractions at high conversion rates. The pilot plant used in this example was the same slurry phase, tubular reactor described in Example 1. In each test, the heavy oil feedstock was thoroughly mixed with up to 250 parts per million of the catalyst precursor over a prolonged period of time before being introduced to the reactor. The reactor temperature was maintained between 430-450° C. to control the conversion level. The reactor pressure was 2000 psig and the hydrogen treat rate was 5000 standard cubic feet per barrel of heavy oil. The results of this test are set forth in Table I below: TABLE I Maya/ Chinese Athabasca Cold Lake Ithmus Paraffinic Feedstock Bitumen Bottoms Blend Bottoms Blend 975° F.+ resid 94 94 63 95 conversion, wt % Asphaltene (C₅ Ins.) 95 93 67 96 conversion wt % Sulfur conversion 78 78 56 92 wt %

This test confirms that a colloidal or molecular catalyst utilized in a slurry phase reactor according to the invention was able to convert the asphaltene fraction at essentially the same rate as the overall resid conversion rate, even at very high overall conversion rates. This demonstrates the superiority of the hydroprocessing methods and systems disclosed herein compared to conventional fixed bed systems, which cannot be operated at conversion levels higher than about 25% when processing reside feedstocks having a significant asphaltene fraction, and conventional ebullated bed systems, which convert asphaltenes at substantially lower conversion levels compared to overall resid conversion, particular at high resid conversion levels. This shows that the methods and systems of the invention satisfy a long-felt need in the art that has not been solved using convention hydroprocessing systems (i.e., being able to convert high asphaltene-containing feedstocks at high conversion levels while also converting the asphaltene fraction at the same conversion level). It is also a surprising and unexpected result given the fact that conventional supported catalysts in existence and used for decades cannot convert the asphaltene and overall resid fractions at the same rate, particularly at high overall conversion levels.

EXAMPLE 4

This example utilized the pilot plant shown in FIG. 10, which included two ebullated bed reactors connected in series and which was used to compare the difference between using a porous supported ebullated bed catalyst (“EB catalyst”) by itself when processing a heavy oil feedstock containing asphaltenes and the EB catalyst in combination with a colloidal or molecular molybdenum disulfide catalyst. A currently-operating commercial ebullated bed unit was simulated in this pilot test. The feedstock for this test was a vacuum tower bottoms generated from a Russian crude in an operating commercial plant, and the EB catalyst was taken from inventory at the same commercial plant. The vacuum tower bottoms contained 90 wt. % of material with a boiling point of 525° C.+ (i.e., greater than or equal to 525° C.). The comparative experiments were carried out at reaction temperature between 418-435° C. to control the conversion level, a space velocity of 0.26 per hour, a hydrogen feed rate of 4500 standard cubic feet per barrel of heavy oil, and a pressure of 2100 psig.

The results of this comparative study are graphically depicted in FIGS. 11-14. The comparative study demonstrated the ability of the colloidal or molecular catalyst to convert asphaltenes to lower boiling materials while also prolonging the useful lifespan of the porous supported catalyst.

The first run (Run “A”) was a base-line test simulating the current commercial unit operation with the EB catalyst, but without the colloidal or molecular catalyst. To simulate real commercial conditions, a mixture of one-third fresh EB catalyst and 2/3 equilibrium EB catalyst taken from the commercial plant was used. The test unit was operated for 5 days at approximately 50 wt % residuum (b.p. ≧524° C.) conversion, and then for 4 days at 58-60 wt % conversion. At the end of the 9-day period, the test had to be shut down because of a significant increase in pressure across the second reactor schematically shown in FIG. 10. At the end of the run, the reactors were opened, the EB catalyst was unloaded, and the reactor walls and all accessories were inspected. Samples were taken and analyzed.

The second test (Run “B”) was a duplication of Run “A”, using an identical catalyst charge (i.e., a mixture of fresh and equilibrium EB catalyst), but with the feedstock conditioned with 25 to 100 ppm of a colloidal or molecular molybdenum sulfide catalyst (i.e., 50 ppm from 0-120 hours; 100 ppm from 120-195 hours; 100 ppm from 195-270 hours; 50 ppm from 270-340 hours, and 25 ppm beyond 340 hours). After operating for 8 days at the same conditions as Run “A”, conversion was increased to 70% and was held at that level for 3 days. The residuum conversion level was then reduced back to 60% and held for 5 days to confirm the reproducibility if the test results. Run “B” was then terminated at the end of this time, with the observation that the unit was fully operable with no noticeable change in pressure drop across the second reactor shown in FIG. 10, even after 16 days on-stream. As in the first test, the reactors were opened and inspected after shutdown.

The pressure drop across the second reactor that caused the shutdown of Run “A”, but which did not occur in Run “B”, is graphically depicted in the chart of FIG. As shown in FIG. 11, Run “A” lasted a little over approximately 220 hours before it was halted due to a dramatic increase in pressure drop across the second reactor resulting from deposition of sediment in the reactor (i.e., equipment fouling). A post-run inspection showed significant fouling of the screen at the reactor liquid recycle cup of the second reactor, which caused the increase in pressure drop between the reactor inlet and outlet. On the other hand, Run “B” lasted about 400 hours and was only halted because all the relevant data had been obtained, not because of any equipment fouling or pressure increase across the second reactor. A post-run inspection showed minimal fouling of the screen at the reactor liquid recycle cup in the second reactor, thus preventing, or at least minimizing, the type of differential pressure increase that occurred in Run “A”.

The chart shown in FIG. 12 plots resid conversion versus hours on-stream. For the first 9 days, the two test runs tracked each other very well. Oily Run “B” was able to continue more than 9 days, however, as described above. As shown in FIG. 12, when the percent conversion was maintained at approximately the same level for both test runs, Run “B” had a substantially higher percent conversion of the resid fraction. This demonstrated that the colloidal or molecular catalyst assisted the EB catalyst in converting the vacuum tower residuum material to lower boiling materials.

The chart depicted in FIG. 13 shows asphaltene conversion (defined in terms of heptane insolubles) versus time on-stream at various resid conversion levels. Run “B”, using the colloidal or molecular catalyst and EB catalyst, achieved approximately twice the asphaltene conversion as in Run “A”, using the EB catalyst alone. This significant improvement in asphaltene conversion is directly attributable to the use of the colloidal or molecular catalyst because, otherwise, the two test runs were identical. This test confirms the results of Example 1, which demonstrated that a colloidal or molecular catalyst is much better able to convert asphaltenes in a heavy oil feedstock than a porous supported catalyst.

The chart depicted in FIG. 14 plots percent desulirization of the residuum as a function of time comparing Run “A” using just the EB catalyst and Run “B” using both the EB catalyst and the colloidal or molecular catalyst.

Table II below summarizes the test data on sediment formation as determined by the IP 375 Method. TABLE II IMPACT OF COLLOIDAL OR MOLECULAR CATALYST ON SEDIMENT FORMATION AND FOULING Residuum conversion 50 60 71 60 wt. % Time On-Stream hours 0 to 132 133 to 220 204 to 272 272 to 400 RUN “A”: Sediment 0.12-0.22 0.59-0.86 N/A N/A wt. % (EB catalyst only) RUN “B”: Sediment 0.06-0.15 0.32-0.36 0.72-1.06 0.23-0.35 wt. % (EB catalyst + C or M catalyst) Run A operated for 220 hours but had to be stopped when the differential pressure in the second reactor increased significantly. No data was generated after 220 hours. A post-run inspection showed significantly fouling on the screen of the reactor liquid recycle cup. Run B operated for 400 hours with very little change in reactor differential pressure. Inspection showed the screen at the reactor liquid recycle cup to be clean with minimal fouling.

The sediment formation values for Run “B” were about half of those from Run “A” during the comparative time periods and reaction conditions. For Run “B”, when-conversion was reduced from 71% to 60% in the last 5 days, sediment values returned to the same range as in the initial 60% conversion, despite any additional EB catalyst deactivation that may have occurred when operating the reactor at 71% conversion. Because sediment was significantly reduced when the colloidal or molecular catalyst was used, the pilot plant unit proved to be less prone to fouling and plugging than when just the conventional EB catalyst was used, as evidenced by the lower pressure drop across the reactor. It can be extrapolated that the same benefits of using the colloidal or molecular catalyst would apply in commercial-scale operations. That is, reduced sediment formation would be expected to lead to less fouling of the equipment and solid supported catalyst which, in turn, would result in longer unit operation and less maintenance when the colloidal or molecular catalyst is used in addition to, or in combination with, the EB catalyst.

In summary, the colloidal or molecular catalyst consistently increased the asphaltene conversion in parallel with the resid conversion and reduced sediment formation. These results demonstrate that the colloidal or molecular catalyst significantly increased hydrogen transfer outside the supported catalyst, capped the free radicals, and minimized combination reactions involving free radicals, as reflected in the reduction of sediment at all levels of resid conversion. Reducing sediment formation reduces rate of deactivation of the supported catalyst. The supported catalyst is therefore able to continue to perform its catalytic function of removing sulfur and transferring hydrogen, resulting in higher API gravity products.

EXAMPLE 5

A test was conducted using the pilot plant describes in FIG. 10, except that the first and second reactors were operated in a slurry phase hydroprocessing system comprising a slurry phase reactor that utilized 125 parts per million of a colloidal or molecular molybdenum disulfide catalyst. (The reactors operated as “slurry phase” reactors in this test rather than ebullated bed reactors because they utilized no porous supported ebullated bed catalyst). The pilot plant operated at 1500 psig of hydrogen pressure, with the conditioned Athabasca resid being fed at a space velocity of 0.7 per hour, a hydrogen treat rate at 4500 standard cubic feet per barrel of resid, within the first reactor being maintained at less than 370° C. and the second reactor being maintained at 441° C. The liquid product was collected and fed into a simulated guard bed reactor packed with a demetalizing catalyst.

The purpose of this test was to determine whether a slurry phase reactor employing a colloidal or molecular molybdenum disulfide catalyst could be used to preliminarily convert resid and asphaltene fractions, as well as metals contained therein to metal sulfides, followed by removing any metal sulfides, including the colloidal or molecular molybdenum disulfide catalyst by the guard bed. This would allow a fixed bed reactor to subsequently carry out desulfirization and denitrogenation of the preliminarily converted feedstock without the risk of plugging the hydrotreating catalyst by metals originally in the feedstock and/or from the added colloidal or molecular molybdenum disulfide catalyst.

In this study, a catalyst precursor composition comprising molybdenum 2-ethylhexanoate (15% molybdenum by weight) was first diluted down to about 1% by weight molybdenum metal using Number 2 fuel oil (heavy diesel). This diluted precursor composition was intimately mixed with Athabasca vacuum tower bottoms to yield a conditioned feedstock, which was heated to 400° C. (752° F.) in a feed heater to form the colloidal or molecular molybdenum disulfide catalyst and then hydrocracked at 440° C. (824° F.) in a pilot gas-liquid slurry phase back-mixed reactor.

The second reactor shown in FIG. 10 had an effective volume of 2,239 ml, a height of 4.27 meters, and an internal diameter of 2.95 cm. The pilot reactor had an external recycle pump to circulate the reactor liquid from the top of the reactor back to the reactor entrance by means of an external loop. Circulating the reactor liquid enabled rapid dissipation of heat generated by hydroprocessing reactions and maintenance of a homogeneous reactor liquid temperature profile. At the reactor entrance, fresh feedstock and hydrogen were joined with the recycled reactor liquid, which then underwent hydrocracking reactions.

Effluent taken from the reactor was introduced into a hot separator, which separated the effluent into a hot vapor and gaseous stream, which was removed from the top, and a liquid product stream, which was removed from the bottom. After cooling and pressure reduction through subsequent downstream separators, the hydrocracked products were collected as light condensates, bottom liquid, product gas, and dissolved gas. The light condensate and bottom liquid were combined as total liquid and fed to the guard bed reactor packed with a commercial demetalization catalyst supplied by WR Grace.

140 grams of demetalization catalyst were utilized within the guard bed unit. The feed rate was 124 g/hr of hydrocracked product from the slurry phase reactor. Operating conditions were 380° C. (716° F.) at 2,000 psi. The hydrogen flow rate was 300 SCF/bbl (standard cubic feet per barrel-42 gallons of liquid feed). The metal analysis of the hydrocracked product from the pilot slurry phase reactor are shown in Table III as follows: TABLE III Concentration Metal (Weight Part Per Million (WPPM)) Nickel 94 Vanadium 260 Molybdenum 134

The metal analysis after the product was demetalized using the guard bed demetalization catalyst is shown in Table IV as follows: TABLE IV Metal WPPM Wt % Removed Nickel 4 95.7 Vanadium 5 98.1 Molybdenum 4 97.0

As plainly shown, fixed bed demetalization resulted in the removal of the vast majority of metals from the upgraded feedstock formed using the colloidal or molecular catalyst within the pilot slurry phase reactor. This shows that preliminary upgrading of a heavy oil feedstock using a colloidal or molecular catalyst can be successfully carried out in order to (i) upgrade asphaltenes and other higher boiling resid hydrocarbons and (ii) convert metals into a form that facilitates their removal by guard bed demetalization so as to prevent fouling of a downstream fixed bed hydrotreating reactor used for desulfirization and denitrogenation. The demetalization catalyst removed both the colloidal or molecular molybdenum disulfide catalyst and the nickel and vanadium fraction found in the feedstock at about the same rate, thereby demonstrating that the colloidal or molecular catalyst could be removed using the same demetalization process typically used to remove metal contaminants from a feedstock. In view of this, one of skill in the art would expect that preliminary upgrading of a heavy oil feedstock rich in asphaltenes can be carried out upstream of a fixed bed hydroprocessing reactor using a colloidal or molecular catalyst, e.g., in one or more of a slurry phase reactor or an ebullated bed reactor, followed by demetalization in a guard bed, in order to eliminate or greatly reduce fouling of a downstream hydrotreating fixed bed reactor by asphaltenes and/or metals found in the feedstock.

EXAMPLE 6

A pilot plant with two ebullated bed reactors connected in series was used to compare the difference between using a porous supported ebullated bed catalyst (“EB catalyst”) by itself when processing a heavy oil feedstock containing asphaltenes and the EB catalyst in combination with a colloidal or molecular molybdenum disulfide catalyst. The pilot plant 900 for this test is schematically depicted in FIG. 10, and included a high shear mixing vessel 902 used to blend molybdenum 2-ethylhexanoate (15% molybdenum by weight of the catalyst precursor composition) into the feedstock to form a conditioned feedstock. The feedstock for this test was 95% Athabasca resid and 5% decant oil from an operating commercial plant, and the EB catalyst was taken from inventory at the same commercial plant. The conditioned feedstock was circulated out and back into the mixing vessel 902 by a pump 904. A high precision metering piston pump 906 drew the conditioned feedstock from the loop and pressurized it to the reactor pressure. Thereafter, hydrogen 908 was fed into the pressurized feedstock and the resulting mixture passed through a pre-heater 910 prior to being introduced into the first of two pilot slurry phase/ebullated bed reactors 912, 912′.

Each of reactors 912, 912′ had an interior volume of 2200 ml and included a porous supported catalyst and a mesh wire guard 914 to keep the supported catalyst within the reactor. The settled height of catalyst in each reactor is indicated by a lower dotted line 916, and the expanded catalyst bed during use is indicated by an upper dotted line 918. The first reactor 912 was loaded with equilibrium catalyst from the second of two LC-Fining reactors in series, while the second reactor 912′ was loaded with ⅓ fresh catalyst and ⅔ equilibrium catalyst from the LC-Fining reactor. The reactors 912, 912′ were operated at a space velocity of 0.28 reactor volume per hour with 2100 psig back pressure. The rate of hydrogen feed was 4500 scf/barrel, with 60% being introduced into the first reactor 912 and 40% being added as supplemental hydrogen 920 to the material being transferred from the first reactor 912 to the second reactor 912′.

During use, either the feedstock only (in the case of Run “A” using an ebullated bed catalyst only) or the feedstock and colloidal or molecular catalyst (in the case of Run “B” using an ebullated bed catalyst and the colloidal or molecular catalyst) were continuous recycled from the top of each reactor to the bottom of the reactor in a manner similar to an actual commercial ebullated bed reactor as it was being upgraded. Upgraded feedstock from the first reactor 912 was transferred together with supplemental hydrogen into the second reactor 912′ for further hydroprocessing. The further upgraded material from the second reactor 912′ was introduced into a first hot separator 922 to separate gases and vapors 924 from a liquid fraction. The liquid 926 from the first hot separator was introduced into a second hot separator 928 to remove additional gases and vapors 924′, which were blended with those from the first hot separator 922 and then separated into gases 930 and condensate 932. The hot separator bottoms 934 were removed from the second hot separator 928.

The first run (Run “A”) was a base-line test simulating the current commercial unit operation with the EB catalyst, but without the colloidal or molecular catalyst. The second test (Run “B”) was a duplication of Run “A”, using an identical catalyst charge (i.e., a mixture of fresh and equilibrium EB catalyst), but with the feedstock conditioned with 50 parts per million of a molybdenum sulfide colloidal or molecular catalyst. For each run, the test unit was operated for 5 days at a reactor temperature of 425° C., followed by 4 days at a temperature of 432-4340° C., and then 1 day at 440° C. Samples were taken from the hot separator bottoms at the end of each 24-hour period and tested.

The results of this comparative study are graphically depicted in FIGS. 15-22. The comparative study demonstrated the ability of the colloidal or molecular catalyst to convert asphaltenes to lower boiling materials while also reducing the formation of sediment in the reactors. It further confirmed the results of the examples above showing that the asphaltene fraction can be converted at the same rate as the overall resid material.

The chart shown in FIG. 15 plots the pressure drop across the second reactor for each of Runs “A” and “B” throughout the duration of the test. The chart shown in FIG. 16 plots resid conversion for Runs “A” and “B” versus hours on stream. Throughout the test, the overall conversion levels for the two types of catalysts were kept about the same. Nevertheless, the chart shown in FIG. 15 shows a greater pressure drop across the second reactor for Run “A” compared to Run “B” throughout the test after the first 24 hours. The greater pressure differential suggests a significantly larger buildup of sediment in the reactors during Run “A” than in Run “B”, which is consistent with lower conversion of asphaltenes in Run “A”.

In fact, the chart depicted in FIG. 17 shows that the asphaltene conversion (defined in terms of heptane (C₇) insolubles) versus time on-stream at various resid conversion levels was substantially higher in Run “B” compared to Run “A”. The asphaltene conversion levels for each of Runs “A” and “B” started out relative high. Thereafter, the asphaltene conversion for Run “B” remained high (i.e., greater than about 85%, while the asphaltene conversion for Run “A” progressively dropped as the test continued. Moreover, the difference between the asphaltene conversion levels for Runs “A” and “B” progressively widened as the test progressed. This demonstrates that the colloidal or molecular catalyst greatly assisted in converting the asphaltene fraction, particularly over time, compared to using the porous supported catalyst by itself.

The chart depicted in FIG. 18 plots the API gravity of the hot separator bottoms for Runs “A” and “B”. The chart depicted in FIG. 19 plots the unconverted resid API gravity for Runs “A”and “B”. The data in both charts are consistent with the overall increase in asphaltene conversion in Run “B” compared to Run “A” and increased hydrogen transfer to the product via the colloidal or molecular catalyst and the less deactivated porous supported catalyst. The reduction in sediment formation slows the deactivation of the supported catalyst, which is clearly demonstrated by the higher API gravity shown in FIGS. 18 and 19. Since API gravity is directly related to quality and hydrogen contents, higher API gravity means higher hydrogen contents and lower absolute specific gravity.

The chart shown in FIG. 20 plots the IP-375 sediment found in the hot separator bottoms for each of Runs “A” and “B”. The chart depicted in FIG. 21 plots the percentage of asphaltenes found in the hot separator bottoms for each of Runs “A” and “B”. The 2-3 fold increase in sediment found in the hot separator bottoms produced in Run “A” compared to Run “B” is consistent with the greater concentration of asphaltenes found in the hot separator bottoms from Run “A”. Moreover, while the concentration of asphaltenes found in the hot separator bottoms from Run “B” remained substantially constant throughout the test, the asphaltenes found in the hot separator bottoms from Run “A” progressively increased over time. This shows that using the colloidal or molecular catalyst would be expected to greatly assist in maintaining steadier levels of asphaltenes in the processed feedstocks, with an attendant reduction in sediment formation compared to using a porous supported catalyst by itself

The chart in FIG. 22 plots the weight percent of micro carbon residue (MCR) found in the hot separator bottoms for each of Runs “A” and “B”. Consistent with the previous data, the MCR in the hot separator bottoms for Run “B” increased throughout the test, while it initially increased then stagnated throughout Run “A”.

The benefits of adding the colloidal or molecular catalyst in addition to the porous supported ebullated bed catalyst compared to using the ebullated bed catalyst by itself can be seen by the follow additional data gleaned from the foregoing test set forth in Table V: TABLE V Catalyst EB Cat. + C or M EB Catalyst Cat. Change 525° C+ Conv. wt % 72.8 81.7 8.9 C₁-C₃, wt % feed 3.9 5.3 1.4 C₄-524° C. Barrel 0.77 0.88 0.11 (2.8° API) product/Barrel feed (34.1° API) (36.9° API) 525° C.+, Barrel 0.25 0.16 −0.09 (−1.5° API) product/Barrel feed (5.8° API) (4.3° API) Conradson Carbon 69.3 76.4 7.1 residue or MCR Conversion C₇ Asph Conv wt % 79.8 88.4 8.6 Sediment after hot 0.03 <0.01 −0.02 filtration test following the blending of 525° C.+ resid with a light crude oil Basic Sediment and 0.2 0.1 −0.1 Water content

The present invention may be embodied in other specific forms without departing from its spirit or essential characteristics. The described embodiments are to be considered in all respects only as illustrative and not restrictive. The scope of the invention is, therefore, indicated by the appended claims rather than by the foregoing description. All changes which come within the meaning and range of equivalency of the claims are to be embraced within their scope. 

1. A method of upgrading a pre-existing fixed bed hydroprocessing system, comprising: (a) operating a pre-existing fixed bed hydroprocessing system comprising one or more fixed bed reactors, each of which comprises a liquid hydrocarbon phase, a bed of a porous supported catalyst as a solid phase, and hydrogen gas as a gaseous phase (b) preparing a heavy oil feedstock by intimately mixing a catalyst precursor composition into the heavy oil feedstock in a manner so that a colloidal or molecular catalyst is formed when the heavy oil feedstock is heated to above the decomposition temperature of the catalyst precursor composition; (c) forming the colloidal or molecular catalyst in situ within the heavy oil feedstock. (d) introducing the heavy oil feedstock from (b), optionally after (c), into at least one of: one or more fixed bed reactors of the pre-existing fixed bed hydroprocessing system to yield an upgraded fixed bed hydroprocessing system comprising one or more fixed bed reactors; or one or more slurry phase reactors to yield an upgraded fixed bed hydroprocessing system comprising one or more fixed bed reactors positioned upstream from one or more fixed bed reactors of the pre-existing fixed bed hydroprocessing system; and (e) operating the upgraded fixed bed hydroprocessing system to form a hydroprocessed feedstock.
 2. A method as defined in claim 1, the pre-existing fixed bed hydroprocessing system being an EXXON RESIDfining system.
 3. A method as defined in claim 1, wherein the catalyst precursor composition comprises an organo-metallic compound or complex.
 4. A method as defined in claim 1, the catalyst precursor composition comprising at least one transition metal and at least one organic moiety comprising or derived from octanoic acid, 2-ethylhexanoic acid, naphthanic acid, pentacarbonyl, or hexacarbonyl.
 5. A method as defined in claim 4, the catalyst precursor composition comprising at least one of molybdenim 2-ethylhexanoate, molybdenum naphthanate, molybdenum hexacarbonyl, vanadium octoate, vanadium naphthanate, or iron pentacarbonyl.
 6. A method as defined in claim 1, wherein the heavy oil feedstock comprises at least one of heavy crude oil, oil sand bitumen, atmospheric tower bottoms, vacuum tower bottoms, resid, visbreaker bottoms, coal tar, heavy oil from oil shale, or liquefied coal.
 7. A method as defined in claim 1, the heavy oil feedstock comprising at least about 5% by weight of asphaltenes.
 8. A method as defined in claim 7, at least a portion of the colloidal or molecular catalyst being associated with at least a portion of the asphaltenes in the hydrocarbon feedstock, the colloidal or molecular catalyst associated with the asphaltenes in the hydrocarbon feedstock promoting reactions between free radicals formed from the asphaltenes and hydrogen during (e), the reactions between the free radicals formed from the asphaltenes and hydrogen reducing or eliminating formation of coke-precursors and sediment.
 9. A method as defined in claim 1, wherein (b) comprises: pre-mixing the catalyst precursor composition with a hydrocarbon oil diluent below the decomposition temperature of the catalyst precursor composition; and mixing the hydrocarbon oil diluent with the heavy oil feedstock.
 10. A method as defined in claim 9, wherein the hydrocarbon oil diluent comprises at least one of vacuum gas oil, decant oil, cycle oil, or light gas oil.
 11. A method as defined in claim 9, the ratio of catalyst precursor composition to hydrocarbon oil diluent being in a range of about 1:500 to about 1:1.
 12. A method as defined in claim 9, the ratio of catalyst precursor composition to hydrocarbon oil diluent being in a range of about 1:150 to about 1:2.
 13. A method as defined in claim 9, the ratio of catalyst precursor composition to hydrocarbon oil diluent being in a range of about 1:100 to about 1:5.
 14. A method as defined in claim 9, the hydrocarbon oil diluent and catalyst precursor composition being mixed at temperature in a range of about 25° C. to about 250° C., the diluted precursor mixture and heavy oil feedstock being mixed at a temperature in a range of about 25° C. to about 350° C., the conditioned feedstock being heated to a temperature in a range of about 275° C. to about 450° C. in order to form the colloidal or molecular catalyst in (c).
 15. A method as defined in claim 9, the hydrocarbon oil diluent and catalyst precursor composition being mixed at temperature in a range of about 50° C. to about 200° C., the diluted precursor mixture and heavy oil, feedstock being mixed at a temperature in a range of about 50° C. to about 300° C., the conditioned feedstock being heated to a temperature in a range of about 350° C. to about 440° C. in order to form the colloidal or molecular catalyst in (c).
 16. A method as defined in claim 9, the hydrocarbon oil diluent and catalyst precursor composition being mixed at temperature in a range of about 75° C. to about 150° C., the diluted precursor mixture and heavy oil feedstock being mixed at a temperature in a range of about 75° C. to about 250° C., the conditioned feedstock being heated to a temperature in a range of about 375° C. to about 420° C. in order to form the colloidal or molecular catalyst in (c).
 17. A method as defined in claim 9, the hydrocarbon oil diluent and catalyst precursor composition being mixed for a time period in a range of about 1 second to about 20 minutes, and the diluted precursor mixture and heavy oil feedstock being mixed for a time period in a range of about 1 second to about 20 minutes.
 18. A method as defined in claim 9, the hydrocarbon oil diluent and catalyst precursor composition being mixed for a time period in a range of about 5 seconds to about 10 minutes, and the diluted precursor mixture and heavy oil feedstock being mixed for a time period in a range of about 5 seconds to about 10 minutes.
 19. A method as defined in claim 9, the hydrocarbon oil diluent and catalyst precursor composition being mixed for a time period in a range of about 20 seconds to about 3 minutes, and the diluted precursor mixture and heavy oil feedstock being mixed for a time period in a range of about 20 seconds to about 5 minutes.
 20. A method as defined in claim 1, wherein (c) occurs before (d).
 21. A method as defined in claim 1, wherein (c) occurs during or after (d).
 22. A method as defined in claim 1, the catalyst metal in the colloidal or molecular catalyst having a concentration in a range of about 10 ppm to about 500 ppm by weight of the heavy oil feedstock in (d).
 23. A method as defined in claim 1, the catalyst metal in the colloidal or molecular catalyst having a concentration in a range of about 25 ppm to about 300 ppm by weight of the heavy oil feedstock in (d).
 24. A method as defined in claim 1, the catalyst metal in the colloidal or molecular catalyst having a concentration in a range of about 50 ppm to about 175 ppm by weight of the heavy oil feedstock in (d).
 25. A method as defined in claim 1, wherein the colloidal or molecular catalyst comprises molybdenum disulfide.
 26. A method as defined in claim 1, further comprising removing at least a portion of the porous supported catalyst from one or more of the fixed bed reactors of the upgraded fixed bed hydroprocessing system.
 27. A method as defined in claim 1, further comprising beginning to operate a slurry phase reactor upstream from at least one fixed bed reactor, the slurry phase reactor comprising the heavy oil feedstock and the colloidal or molecular catalyst as a liquid phase and hydrogen gas as a gaseous phase.
 28. A method as defined in claim 27, the slurry phase reactor comprising a new reactor that is constructed upstream from the at least one fixed bed reactor.
 29. A method as defined in claim 28, the new reactor comprising a recycle channel, recycling pump, and a distributor grid plate.
 30. A method as defined in claim 27, the slurry phase reactor comprising a former fixed bed reactor of the pre-existing fixed bed hydroprocessing system that has been converted into the slurry phase reactor of the upgraded fixed bed hydroprocessing system by removing the porous supported catalyst from the former fixed bed reactor.
 31. A method as defined in claim 30, further comprising re-routing the heavy oil feedstock in order to initially by-pass a guard bed initially positioned upstream from the former fixed bed reactor that was converted into the slurry phase reactor so that the heavy oil feedstock is introduced into the slurry phase reactor prior to being introduced into the guard bed.
 32. A method as defined in claim 31, the guard bed removing at least a portion of the colloidal or molecular catalyst and metal impurities from the upgraded feedstock and thereby form a cleaned material.
 33. A method as defined in claim 32, further comprising introducing the cleaned material from the guard bed reactor into one or more fixed bed reactors of the pre-existing fixed bed hydroprocessing system and hydrotreating the cleaned material to form a hydrotreated product.
 34. An upgraded fixed bed hydroprocessing system resulting from the method of claim
 1. 35. A method of upgrading a pre-existing fixed bed hydroprocessing system, comprising: (a) operating a pre-existing fixed bed hydroprocessing system comprising one or more fixed bed reactors, each of which comprises a liquid hydrocarbon phase, a bed of a porous supported catalyst as a solid phase, and hydrogen gas as a gaseous phase; and (b) constructing and operating one or more slurry phase reactors upstream from at least one fixed bed reactor of the pre-existing fixed bed hydroprocessing system in order to form an upgraded feedstock from a heavy oil feedstock, each slurry phase reactor comprising a liquid phase comprised of a heavy oil feedstock and a colloidal or molecular catalyst and a gaseous phase comprised of hydrogen gas, the colloidal or molecular catalyst being prepared by: (1) intimately mixing a catalyst precursor composition into the heavy oil feedstock in a manner so that the colloidal or molecular catalyst is formed upon heating the heavy oil feedstock to above the decomposition temperature of the precursor composition; and (2) forming the colloidal or molecular catalyst in situ within the heavy oil feedstock; and (c) introducing the upgraded feedstock from the slurry phase reactor into at least one fixed bed reactor of the pre-existing fixed bed hydroprocessing system to yield an upgraded fixed bed hydroprocessing system comprising one or more slurry phase reactors in combination with the one or more fixed bed reactors.
 36. A method as defined in claim 35, further comprising: introducing the upgraded feedstock from (b) into a guard bed reactor in order to remove at least a portion of the colloidal or molecular catalyst and metal impurities from the upgraded feedstock and thereby form a cleaned material; and introducing the cleaned material into one or more fixed bed reactors according to (c) and hydrotreating the cleaned material to yield a hydrotreated material.
 37. A method of upgrading a pre-existing fixed bed hydroprocessing system, comprising: (a) operating a pre-existing fixed bed hydroprocessing system comprising one or more pre-existing fixed bed reactors, each of which comprises a liquid hydrocarbon phase, a bed of a porous supported catalyst as a solid phase, and hydrogen gas as a gaseous phase; and (b) converting at least one pre-existing fixed bed reactor into a slurry phase reactor to yield an upgraded fixed bed hydroprocessing system comprising one or more converted slurry phase reactors in combination with one or more remaining fixed bed reactors, each slurry phase reactor comprising a liquid phase comprised of a heavy oil feedstock and a colloidal or molecular catalyst and a gaseous phase comprised of hydrogen gas, the colloidal or molecular catalyst being prepared by: (1) intimately mixing a catalyst precursor composition into the heavy oil feedstock in a manner so that the colloidal or molecular catalyst is formed upon heating the heavy oil feedstock to above the decomposition temperature of the precursor composition; and (2) forming the colloidal or molecular catalyst in situ within the heavy oil feedstock.
 38. A method as defined in claim 37, further comprising: introducing an upgraded feedstock from the one or more converted slurry phase reactors into a guard bed reactor in order to remove at least a portion of the colloidal or molecular catalyst and metal impurities from the upgraded feedstock and thereby form a cleaned material; and introducing the cleaned material into the one or more remaining fixed bed reactors and hydrotreating the cleaned material to yield a hydrotreated material.
 39. A method as defined in claim 38, the guard bed reactor comprising part of the pre-existing fixed bed hydroprocessing system.
 40. A method of hydroprocessing a heavy oil feedstock, comprising: preparing a heavy oil feedstock comprised of a substantial quantity of hydrocarbons having a boiling point greater than about 650° F. and a colloidal or molecular catalyst dispersed throughout the feedstock; heating or maintaining the heavy oil feedstock at a hydrocracking temperature within one or more slurry phase reactors to yield an upgraded material; introducing the upgraded material into a guard bed reactor in order to remove at least a portion of the colloidal or molecular catalyst and metal impurities from the upgraded feedstock and thereby form a cleaned material; and hydrotreating the cleaned material within one or more fixed bed hydrotreating reactors to yield a hydrotreated material.
 41. A method as defined in claim 40, the one or more slurry phase reactors achieving at least about 50% conversion of the heavy oil feedstock, including at least about 50% conversion of any asphaltenes contained therein.
 42. A method as defined in claim 40, the one or more slurry phase reactors achieving at least about 65% conversion of the heavy oil feedstock, including at least about 65% conversion of any asphaltenes contained therein.
 43. A method as defined in claim 40, the one or more slurry phase reactors achieving at least about 80% conversion of the heavy oil feedstock, including at least about 80% conversion of any asphaltenes contained therein.
 44. A fixed bed hydroprocessing system, comprising: a slurry phase reactor that comprises a liquid hydrocarbon phase comprised of a heavy oil feedstock and a colloidal or molecular catalyst and a gaseous phase comprised of hydrogen gas and that yields an upgraded material from the heavy oil feedstock; a guard bed reactor positioned downstream from the slurry phase reactor that removes at least a portion of the colloidal or molecular catalyst and metal impurities from the upgraded feedstock and thereby form a cleaned material; and a fixed bed hydrotreating reactor positioned downstream from the guard bed reactor that hydrotreats the cleaned material to yield a hydrotreated material. 